CN108128829A - Taurine waste water zero discharge treatment process and taurine wastewater zero discharge processing unit - Google Patents
Taurine waste water zero discharge treatment process and taurine wastewater zero discharge processing unit Download PDFInfo
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- CN108128829A CN108128829A CN201810142078.5A CN201810142078A CN108128829A CN 108128829 A CN108128829 A CN 108128829A CN 201810142078 A CN201810142078 A CN 201810142078A CN 108128829 A CN108128829 A CN 108128829A
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- taurine
- waste water
- pretreater
- zero discharge
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- XOAAWQZATWQOTB-UHFFFAOYSA-N taurine Chemical compound NCCS(O)(=O)=O XOAAWQZATWQOTB-UHFFFAOYSA-N 0.000 title claims abstract description 185
- 239000002351 wastewater Substances 0.000 title claims abstract description 102
- 229960003080 taurine Drugs 0.000 title claims abstract description 93
- 238000000034 method Methods 0.000 title claims abstract description 57
- 238000012545 processing Methods 0.000 title claims abstract description 45
- 208000028659 discharge Diseases 0.000 title claims abstract description 39
- 230000008569 process Effects 0.000 title claims abstract description 37
- 238000011282 treatment Methods 0.000 title claims abstract description 37
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 89
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 claims abstract description 48
- 239000000126 substance Substances 0.000 claims abstract description 48
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 45
- 239000007789 gas Substances 0.000 claims abstract description 41
- 239000007791 liquid phase Substances 0.000 claims abstract description 38
- ROSDSFDQCJNGOL-UHFFFAOYSA-N Dimethylamine Chemical compound CNC ROSDSFDQCJNGOL-UHFFFAOYSA-N 0.000 claims abstract description 36
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 26
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 25
- 239000012071 phase Substances 0.000 claims abstract description 25
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical class [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 17
- 238000011033 desalting Methods 0.000 claims abstract description 13
- 150000003839 salts Chemical class 0.000 claims abstract description 13
- 235000011130 ammonium sulphate Nutrition 0.000 claims abstract description 12
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims abstract description 11
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims abstract description 11
- 238000010612 desalination reaction Methods 0.000 claims abstract description 11
- 238000012958 reprocessing Methods 0.000 claims abstract description 7
- 238000010992 reflux Methods 0.000 claims description 39
- 238000007670 refining Methods 0.000 claims description 26
- 238000001704 evaporation Methods 0.000 claims description 17
- 230000008020 evaporation Effects 0.000 claims description 15
- 239000000908 ammonium hydroxide Substances 0.000 claims description 14
- 230000000694 effects Effects 0.000 claims description 11
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 238000004064 recycling Methods 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 6
- 238000009834 vaporization Methods 0.000 claims description 3
- 230000008016 vaporization Effects 0.000 claims description 3
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 claims description 2
- GWZOLWLJEJRQMZ-UHFFFAOYSA-N [S].S Chemical compound [S].S GWZOLWLJEJRQMZ-UHFFFAOYSA-N 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 40
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 abstract description 30
- 239000000203 mixture Substances 0.000 abstract description 6
- 239000007792 gaseous phase Substances 0.000 abstract description 3
- 238000004519 manufacturing process Methods 0.000 description 25
- 235000011114 ammonium hydroxide Nutrition 0.000 description 14
- 238000005516 engineering process Methods 0.000 description 14
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 13
- 239000000047 product Substances 0.000 description 13
- 238000004065 wastewater treatment Methods 0.000 description 11
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 description 6
- 230000008859 change Effects 0.000 description 6
- 229940031098 ethanolamine Drugs 0.000 description 6
- 238000000605 extraction Methods 0.000 description 6
- 239000006227 byproduct Substances 0.000 description 4
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000004821 distillation Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- -1 feed Substances 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- 238000011144 upstream manufacturing Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 150000002576 ketones Chemical class 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 125000001477 organic nitrogen group Chemical group 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 2
- 235000011152 sodium sulphate Nutrition 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 238000004176 ammonification Methods 0.000 description 1
- UYJXRRSPUVSSMN-UHFFFAOYSA-P ammonium sulfide Chemical compound [NH4+].[NH4+].[S-2] UYJXRRSPUVSSMN-UHFFFAOYSA-P 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 210000001367 artery Anatomy 0.000 description 1
- 230000003851 biochemical process Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000005282 brightening Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 235000021443 coca cola Nutrition 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000000909 electrodialysis Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 235000013373 food additive Nutrition 0.000 description 1
- 239000002778 food additive Substances 0.000 description 1
- 238000001640 fractional crystallisation Methods 0.000 description 1
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical group O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000020477 pH reduction Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 229940079827 sodium hydrogen sulfite Drugs 0.000 description 1
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 description 1
- 235000010265 sodium sulphite Nutrition 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 description 1
- 210000003462 vein Anatomy 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
Classifications
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/24—Sulfates of ammonium
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
- C07C209/82—Purification; Separation; Stabilisation; Use of additives
- C07C209/86—Separation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/78—Separation; Purification; Stabilisation; Use of additives
-
- 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
- C02F2103/36—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 manufacture of organic compounds
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Inorganic Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Physical Water Treatments (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of taurine waste water zero discharge treatment process, including step 1, desalting processing, taurine waste water are carried out desalting processing first, removes salts substances therein, obtain desalination taurine waste water；The pretreatment of step 2, the desalination taurine waste water detaches the desalination taurine waste water through rectifying column, and top gaseous phase obtains the mixture of hydrogen sulfide, ammonia, and tower reactor obtains low ammonia nitrogen value waste water；Step 3 is passed through saturated ammonia water wash column in the pending substance of gas phase, reacts to form ammonium sulfate with the hydrogen sulfide in the taurine waste water；The reprocessing of step 4, the pending substance of the liquid phase; the pending substance of the liquid phase is subjected to rectification process in rectifying column and isolates dimethylamine and acetone; the COD value of taurine waste water can be achieved; pH value, ammonia nitrogen value is up to standard simultaneously, by processed waste water fully recovering; all cycle water zero discharges; zero emission effectively by resource maximum utilizationization, reduces the pollution of environment.
Description
Technical field
The present invention relates to field of fine chemical, and in particular to taurine waste water treatment process and its equipment.
Background technology
Taurine is widely used in the fields such as medicine, food additives, feed, surfactant and brightening agent, and should
Expanded increasingly with range, be constantly in the state that supply falls short of demand in recent years, by it is widely known be exactly Coca-Cola, red ox, arteries and veins
The necessary additive of all drinks such as dynamic.
At present, taurine is substantially to be produced using the method for chemical synthesis, although the synthesis side of document report taurine
There are many method, but industrial mainly using two methods production taurine：Ethanol amine technique and ethylene oxide process.Ethanol amine technique
It is using monoethanolamine as raw material, is esterified through the concentrated sulfuric acid, sodium sulfite restores and isolates and purifies to obtain taurine product.Ethylene oxide
Technique be using ethylene oxide as starting material, through with sodium hydrogensulfite addition, then through ammonification, neutralize, isolate and purify to obtain ox
Sulfonic acid product (Wu meets, the production of Zhu Shengdong taurines and market [J] finely with specialty chemicals -2010 (5) .-1-3).Table 1
Give the concrete principle comparison of both existing taurine production technology：
1 two kinds of taurine production technology contrast tables of table
The characteristics of wherein using ethanol amine technique is technology maturation, and equipment requirement is simple；Shortcoming is that yield is low, production cost
Height, it is seriously polluted.This technique is the traditional processing technology of taurine, and the most of taurine manufacturers of Japan and China use
This technique productions taurine.And the characteristics of ethylene oxide process is with high content of technology, production cost is low (lower than ethanol amine technique big
About 5000 yuan/t), pollution is small, equipment and controlled level is required high.The technique is since production cost is low, and environmental pollution is small, just
Gradually replacing traditional ethanol amine technique, and as the mainstream production technology of taurine.
From the existing taurine production technology introduction described in table 1 it is found that either ethanol amine technique and ethylene oxide process,
The last one step of finished product reaction is product taurine, sodium sulfate byproduct and a large amount of water.Therefore next purifying step
It is consistent at home, be exactly using multiple-effect evaporation, after a large amount of water evaporations are gone out (10,000 tons/year of scale wastewaters are about 300 tons/
My god) so that mother liquor saturation, fractional crystallization obtain product taurine and sodium sulphate respectively.Taurine generates high after washing
Salt waste water (10,000 tons/year of about 5 ton days of scale).Production waste water contains high concentration COD, NH4+-N, organic nitrogen and ammonium sulfate or chlorine
Change the salts such as ammonium.
Many research work have been done to taurine production wastewater treatment by the country at present, such as electrodialysis, liquid-film method, waste water resource
The treatment technologies such as change.But since these technical finesses are of high cost, anti impulsion load is poor, effluent quality does not reach requirement, in work
It is restricted in Cheng Yingyong.Therefore, it at present in industrialized technology, collects processing respectively to waste water and then is integrated using biochemical process
The technology path of improvement is common approach (the commonplace pavilion of Pan, Wang Jiucheng, the Han Yue catalyzed internal electrocatalysis/water for handling taurine production waste water
Solve acidification/UASB/AO/ oxidation coupling flocculation treatments taurine production waste water [J] Treatment of Industrial Water 2015.35 (9)：96-99).
However, for the taurine device of 10,000 scales, handled using ethylene oxide process, 5 ton day (saliferous of high-concentration waste water can be generated
22%wt, ammonia nitrogen value 30000, COD value 18000), 300 ton day of low concentration wastewater (2000-3000 containing COD value, ammonia nitrogen value 100-
300, pH value 10-11.5), the wastewater treatment of such great number, great pressure can be brought with environmental protection by expanding to enterprise.Using cycle
Water, 0.8 yuan/ton of direct cost, 12 yuan/ton of calculating of sewage disposal expense, the direct cost of above-mentioned low concentration wastewater is 126.7 ten thousand
Member/year, after considering the various installations and facilities such as pump, pretreatment pond, cost will be up to 3,500,000 yuan/year, in addition high-concentration waste
Water process, entire project is per about 4,000,000 yuan of annual operating and maintenance cost.Area lacked for water resource, the source of recirculated water is also one urgently
Problem to be solved.
In addition patent of invention [number of patent application：201510806182.6] in disclose a kind of taurine wastewater treatment work
Skill, the technique are to employ the processing of three-level biofermentation method, are arranged outside processed waste water, the investment of energy consumption is huge；Another hair
Bright patent [number of patent application：201220508572.7] a kind of technique concentrated using multiple-effect evaporation is disclosed, which is
The waste water of high ammonia nitrogen with high salt using multiple-effect evaporation is concentrated, after evaporation overhead vapours condensation, still can be become above-mentioned low
Concentration waste water, because of light boiling organics in evaporation process, the ammonia nitrogen that dissociates can enter in vapor, so a large amount of waste water is also
It is to need to pass out to battery limit (BL) waste water treatment plant, which reacts for the final step that existing industrialized unit generally uses
Concentrator does not eliminate the generation of a large amount of waste water in principle.
In view of above-mentioned existing taurine wastewater treatment there are the defects of, the present inventor be based on be engaged in such product design
Manufacture abundant for many years practical experience and professional knowledge, and coordinate the utilization of scientific principle, actively it is subject to research and innovation, to found one
Kind taurine waste water treatment process and its equipment make it have more practicability.By constantly studying, designing, and through trying repeatedly
After making sample and improving, the present invention having practical value is created finally.
Invention content
It is a primary object of the present invention to overcome and fail to realize wastewater zero discharge existing for existing taurine wastewater treatment
The defects of, and a kind of taurine waste water treatment process and its equipment are provided, investment is small, low energy consumption, eliminates original technique to environment
While pollution, high value-added product is recycled, thus more suitable for practicality, and with the utility value in industry.
The object of the invention to solve the technical problems is realized using following technical scheme.
Taurine waste water zero discharge treatment process, includes the following steps：
Taurine waste water is carried out desalting processing, removes salts substances therein, taken off by step 1, desalting processing first
Salt taurine waste water；
The desalination taurine obtained in the step 1 is given up in the pretreatment of step 2, the desalination taurine waste water
Water forms the pending substance of gas phase and the pending substance of liquid phase after reboiler vaporization process；
The reprocessing of step 3, the pending substance of the gas phase is passed through saturation ammonium hydroxide in the pending substance of gas phase, with institute
The hydrogen sulfide stated in taurine waste water reacts to form ammonium sulfate；
The pending substance of the liquid phase is carried out essence by the reprocessing of step 4, the pending substance of the liquid phase in rectifying column
It evaporates processing and isolates dimethylamine and acetone.
As a kind of perferred technical scheme, it is taken off in the step 1 using triple effect evaporation or MVR evaporatings
Salt treatment.
As a kind of perferred technical scheme, pretreatment is carried out in pretreater in the step 2, and the pretreater
In operating pressure be 0.1-1.5MPa, reflux ratio 0.1-50, tower top operation temperature are 10-80 DEG C.
As a kind of perferred technical scheme, the step 3 carries out in ammonia refining tower, and the operation of the ammonia refining tower
Pressure is equal to or less than the operating pressure of the pretreater, operation temperature is 5-50 DEG C.
As a kind of perferred technical scheme, the circulated sprinkling flow of saturation ammonium hydroxide described in the step 3 and the gas
The liquid-gas ratio for treating each other treated substance is 1-10L/Nm3。
As a kind of perferred technical scheme, the tower top operating pressure of rectifying column described in the step 4 is 0.1-
0.4MPa, tower top temperature are 30-60 DEG C, reflux ratio 0.1-15.
Taurine wastewater zero discharge processing unit, including：
Pretreatment unit including pretreater, provides the reboiler of heat to the pretreatment and is arranged on described pre-
Condensation reflux unit at the top for the treatment of column；
Gas-treatment means, including ammonia refining tower, for by the pretreater treated the pending object of gas phase
Hydrogen sulfide reaction generation ammonium sulfate product in matter；
Liquid-phase treatment apparatus including rectifying column, is connect with the pretreater outlet at bottom.
As a kind of perferred technical scheme, the condensation reflux unit includes：
Pretreater condenser is connect with the pretreater top exit, for condensing by the pretreater
The pending substance of gas phase after reason simultaneously generates liquid-phase reflux substance；
Pretreater return tank is connect with the pretreater condenser, for recycling the liquid-phase reflux substance；
Pretreater reflux pump is connect respectively with the pretreater return tank with the pretreater, for by described in
It is returned in the pretreater after the supercharging of liquid-phase reflux substance.
As a kind of perferred technical scheme, the gas-treatment means further include ammonia refining cooler, described for giving
Ammonia refining tower carries out cooling processing.
As a kind of perferred technical scheme, the liquid-phase treatment apparatus further includes：
Rectifying column condenser is arranged on the rectifying column tower top, for condensing the rectifying column tower top steam；
Rectifying return tank is connect with the rectifying column condenser, is handled for recycling by the rectifying column condenser
The liquid phase arrived；
Rectifying reflux pump is connect respectively with the rectifying return tank, the rectifying column, for by the liquid-phase reflux to institute
It states in rectifying column.
Using above-mentioned technical proposal, following technique effect can be realized：
1), taurine waste water zero discharge treatment process flow disclosed by the invention is simple, will directly send to biochemical place originally
The waste water of reason is by device ammonia nitrogen removal and after recycling acetone so that the COD value of waste water, pH value, ammonia nitrogen value is up to standard simultaneously, owns
Water zero discharge is recycled, zero emission effectively by resource maximum utilizationization, reduces the pollution of environment, simple for process, and device is thrown
It provides low, belongs to environmentally friendly technology, material is corrosion-free to equipment, and low energy consumption, has a extensive future；
2nd, taurine waste water zero discharge treatment process can not only be used for single column use, can also multitower use, for high and low
COD value, high and low ammonia nitrogen value, the waste water of high and low pH value can according to field condition with waste water situation reasonable combination technological process,
So that investment is minimum, Income Maximum, environmental pollution is reduced to zero；
3rd, taurine wastewater zero discharge processing unit totally takes up little area, and the complete use of skid, skid can set as a whole
Standby simple in structure, the advantages of with with walking, investment is low, and operating cost is low, and product purity is high, is suitble to serialization, semicontinuous, rule
Modelling produces；
4th, according to 10,000 tons/year of production scales, 4,000,000 yuan/year of production cost, acetone, ammonia and the section of by-product can be saved
2,000,000 yuan/year of sewage treatment equipment facility expense about can be the direct yield that enterprise brings 6,000,000 yuan/year every year, thus
It can be seen that its prospect is superior；
Description of the drawings
Fig. 1 is the structure diagram of taurine wastewater zero discharge processing unit of the present invention；
Structure diagrams of the Fig. 2 for 1 use device of embodiment；
Structure diagrams of the Fig. 3 for 2 use devices of embodiment；
Wherein, 1- pretreaters, 2- pretreater condensers, 3- pretreater return tanks, 4- pretreater reflux pumps, 5-
Reboiler, 6- booster pumps, 7- ammonia refining towers, 8- coolers, 9- ammonia refining return tanks, 10- ammonia refining coolers, 11- circulating pumps,
12- rectifying columns, 13- rectifying column condensers, 14- rectifying return tanks, 15- rectifying reflux pumps；
A- taurine waste water, B- ammonias, C- ammonium sulfates, D- product acetones, E- qualified waters, F- saturation ammonium hydroxide, G- can
Burn exhaust steam,
Specific embodiment
The technological means and effect taken further to illustrate the present invention to reach predetermined goal of the invention, to according to this
Invent the taurine waste water zero discharge treatment process proposed and taurine wastewater zero discharge processing unit its specific embodiment, spy
Sign and its effect are described in detail as after.
The invention discloses a kind of taurine waste water zero discharge treatment process, include the following steps：
Step 1, desalting processing, due to containing high concentration COD, NH4-N, organic nitrogen and ammonium sulfate or chlorine in taurine waste water
Change the salts such as ammonium, be high COD, high ammonia nitrogen, high-salt wastewater, need first to be removed salt therein, specifically, taurine is given up
Water carries out desalting processing first, removes salts substances therein, obtains desalination taurine waste water；
The pretreatment of step 2, desalination taurine waste water, by the desalination taurine waste water obtained in step 1 through 5 vapour of reboiler
The pending substance of gas phase and the pending substance of liquid phase are formed after change processing；
The reprocessing of the pending substance of step 3, gas phase is passed through saturation ammonium hydroxide, with taurine in the pending substance of gas phase
Hydrogen sulfide in waste water reacts to form ammonium sulfate, due to saturation ammonium hydroxide no longer absorbs ammonia and hydrogen sulfide is sour gas, with ammonia
Water reaction generation ammonium sulfide, therefore reacted using saturation ammonium hydroxide with hydrogen sulfide micro in waste water, byproduct of ammonium sulfate is generated, together
When the tail gas that is formed be more than the high-purity ammon of 99%wt for purity, can return in taurine production system and continue as synthesis ox sulphur
Used in acid, and the taurine waste water zero discharge treatment process can realize tail gas zero-emission；
The reprocessing of the pending substance of step 4, liquid phase, for waste water after the processing of pretreater 1, obtained liquid phase is pending
The ammonia nitrogen value of substance is in 0-10ppm, and pH value is between 7-8, and COD is not changed, therefore is treated liquid phase using rectifying column 12
Treated substance carries out rectifying and isolates dimethylamine and acetone, and the pending substance of liquid phase is specifically carried out rectifying in rectifying column 12
Dimethylamine and acetone are isolated in processing, are 0-50ppm, therefore the tower top of rectifying column 12 can be straight since the input of dimethylamine is less
Crude acetone solution is obtained to obtain, and its purity is 99.6%wt, technical purity can be directly reached, therefore in this process without dividing
From if you need to obtain the acetone of higher purity, further distillation processing can be carried out.After rectification process, dimethylamine and third
Ketone is guessd out in 12 tower top of rectifying column, and ammonia nitrogen value is within 0-5ppm in tower reactor qualified water, and COD value is within 0-20, and pH value is in 7-
Within 7.5, qualified water meets industry water requirement, is recycled in direct reuse to taurine production system.
As a kind of perferred technical scheme, desalting processing is carried out using triple effect evaporation processing unit in step 1, evaporation
(waste water is distillation waste water to a large amount of waste water directly evaporated in condensed water and taurine production process, therefore does not contain salt, can
Directly carry out lower step pretreatment) it is directly mixed into next-step operation step.
As a kind of perferred technical scheme, pretreatment carries out, and the behaviour in pretreater 1 in pretreater 1 in step 2
As pressure be 0.1-1.5MPa, reflux ratio 0.1-50, tower top operation temperature are 10-80 DEG C, it is preferred that in pretreater 1
Operating pressure is 0.1-0.5MPa, reflux ratio 1-10, tower top operation temperature are 15-50 DEG C, wherein, the reality of pretreater 1
Operating pressure is consistent with upstream waste water to be advisable, and tower top operation temperature should be suitable, and the excessively high gas phase for easily causing tower top formation is pending
Steam content is high in substance, increases downstream processes burden, temperature is too low, and pretreating effect is bad, the pending object of liquid phase of discharge
Ammonia nitrogen value in matter is higher, is unable to reach discharge standard.
As a kind of perferred technical scheme, step 3 carries out in ammonia refining tower 7, and the operating pressure of ammonia refining tower 7 is small
In or equal to the operating pressure of pretreater 1, operation temperature be 5-50 DEG C, since its operating pressure is less than or equal to pretreater
1 operating pressure, there is no need to the equipment such as wind turbine, compressor to carry out pressurized treatment.
As a kind of perferred technical scheme, in order to ensure hydrogen sulfide absorption effect, the cycle spray of saturation ammonium hydroxide in step 3
The liquid-gas ratio for drenching flow and the pending substance of gas phase is 1-10L/Nm3, it is preferred that it is 2-6L/Nm3。
As a kind of perferred technical scheme, the tower top operating pressure of rectifying column 12 is 0.1-0.4MPa, tower top in step 4
Temperature is 30-60 DEG C, reflux ratio 0.1-15, it is preferred that the tower top operating pressure of rectifying column 12 is 0.1-0.25MPa, tower top
Temperature is 30-45 DEG C, reflux ratio 0.1-5.
The invention also discloses a kind of taurine wastewater zero discharge processing unit, as shown in Figure 1, including：
Pretreatment unit provides the reboiler 5 of heat including pretreater 1, to pretreatment and is arranged on pretreater 1
The condensation reflux unit at top, pretreatment unit are gentle for that will form the pending substance of liquid phase after taurine waste water vaporization process
Treated substance is treated each other, so as to which the salts substances in taurine waste water be further processed with gas phase discharge；
Gas-treatment means, including ammonia refining tower 7, for by treated the pending substance of gas phase of pretreater 1
In hydrogen sulfide reaction generation ammonium sulfate product；
Liquid-phase treatment apparatus including rectifying column 12, connect with 1 outlet at bottom of pretreater, is mainly used for pretreater 1
The pending substance of liquid phase of discharge carries out rectifying, forms dimethylamine and acetone, and taurine life can be directly connected to by addition discharging waste water
Recycling is carried out into system.
As a kind of perferred technical scheme, condensation reflux unit includes：
Pretreater condenser 2 is connect with 1 top exit of pretreater, and for condensing, by pretreater 1, treated
The pending substance of gas phase simultaneously generates liquid-phase reflux substance；
Pretreater return tank 3 is connect with pretreater condenser 2, for reclaim liquid phase reflux materials；
Pretreater reflux pump 4 is connect respectively with pretreater return tank 3 with pretreater 1, for by liquid-phase reflux object
Matter is returned after being pressurized by booster pump 6 in pretreater 1.
As a kind of perferred technical scheme, since ammonia and hydrogen sulfide are exothermic reaction, and heat accumulates in ammonia refining tower 7
It is interior to be discharged in time, it easily causes internal-response and slows, influence reacting, and under high temperature for saturation ammonium hydroxide and hydrogen sulfide
Vapor entrainment is serious, and it is unfavorable that downstream is produced, therefore gas-treatment means further include ammonia refining cooler 10, for giving ammonia essence
Tower 7 processed carries out cooling processing.In addition the ammonium hydroxide after saturation ammonium hydroxide discharge ammonium sulfate byproduct after being reacted with hydrogen sulfide is by following
Ring pump 11 carries out cycling and reutilization, and judge by pH value in the reaction end of ammonia refining tower 7, has been reacted when saturation ammonium hydroxide is close
When complete, pH value is reduced between 7-11 in system, operational control value 8-9, ensures that system in alkalinity, does not have hydrogen sulfide
It is entrained in taurine production system.
As a kind of perferred technical scheme, liquid-phase treatment apparatus further includes：
Rectifying column condenser 13 is arranged on 12 tower top of rectifying column, for condensing 12 overhead vapours of rectifying column；
Rectifying return tank 14 is connect with rectifying column condenser 13, is obtained for recycling by the processing of rectifying column condenser 13
Liquid phase；
Rectifying reflux pump 15 is connect respectively with rectifying return tank 14, rectifying column 12, for by liquid-phase reflux to rectifying column 12
In.
As a kind of perferred technical scheme, in order to further reduce qualified ammonia entrainment saturated water, cooler is further included
8, for carrying out cooling treatment to the ammonia after refining, it is 5-25 DEG C that cooler 8, which controls cooling temperature, and optimal value is 5-15 DEG C,
The saturated water to cool down enters in ammonia refining return tank 9, is conveyed after saturated water liquid level height to certain value by valve opening
Into ammonia refining tower 7, the ammonia purity come out by ammonia refining tower 7 can be returned directly to taurine production in more than 99%wt
It is applied mechanically in system.
In actual use, 12 tower top of rectifying column can directly obtain crude acetone solution, and its purity can reach 99.6%wt,
Reach technical purity, the acetone that common distillation obtains higher purity in addition can be used.
Differ additionally, due to the effluent water quality of taurine production system output, therefore need to be according to actual demand to above device
It is adaptively adjusted.Specifically, including following two situations：
1st, low ammonia nitrogen, low COD：Since hydrogen sulfide, ammonia-nitrogen content are less in charging, the present invention can also be according to commercial plant
Actual conditions optimize, such as when ammonia nitrogen value is relatively low, while COD value is not also high, the third of device fully recovering at this time
When ketone, dimethylamine Isoquant deficiency production cost, single column, that is, pretreater 1, pretreatment can be directly used at this time
Tower condenser 2, pretreater return tank 3, pretreater reflux pump 4 and reboiler 5 control tower top pressure 0.1-1.5MPa, real
Border pressure is consistent with upstream multiple-effect evaporation pressure, optimum pressure 0.12-0.5MPa, and tower top temperature controls 10-70 DEG C, optimal temperature
It is 40-70 DEG C to spend, theoretical plate 15-85 blocks, and optimal value is 38-65 blocks, and charging Board position is related with feed composition and temperature, tower top
All extraction ammonia, hydrogen sulfide, dimethylamine, acetone steam go burning disposal to gas phase, and tower reactor directly obtains qualified water and applies mechanically.
2nd, low ammonia nitrogen, high COD：Due to hydrogen sulfide in charging, ammonia nitrogen is less, and the present invention can also be according to the reality of commercial plant
Border situation optimizes, such as when ammonia nitrogen value is relatively low while COD value is higher, at this time the ammonia of device fully recovering, sulphur
When changing hydrogen Isoquant deficiency production cost, the above-mentioned taurine wastewater zero discharge processing other than ammonia refining may be used
Device or using single column, that is, pretreater 1, carries out side take-off product acetone, is shared with incineration system.For list
Tower side take-off technique, that is, pretreater 1, pretreater condenser 2, pretreater return tank 3, pretreater reflux pump
4 and reboiler 5, tower top pressure 0.1-1.5MPa is controlled, actual pressure is consistent with upstream multiple-effect evaporation pressure, and optimum pressure is
0.12-0.5MPa, tower top temperature control 10-70 DEG C, and Optimal Temperature is 40-70 DEG C, theoretical plate 35-95 blocks, optimal value 46-75
Block, charging Board position is related with feed composition and temperature, and top gaseous phase all produces ammonia, hydrogen sulfide, side line in 7-33 blocks, most
Excellent position produces dimethylamine, product acetone for 8-20 blocks, and tower reactor directly obtains qualified water and applies mechanically.
In order to further illustrate the present invention, with reference to specific embodiment to taurine wastewater zero discharge provided by the invention
Treatment process and taurine wastewater zero discharge processing unit are described in detail, but should not be construed as protecting the present invention
The restriction of range.
Embodiment 1
Taurine waste water (carries out the condensed water evaporated after desalting processing to produce with taurine using triple effect evaporation processing unit
The waste water that a large amount of waste water directly evaporated in the process obtain after merging)：COD value is 1130, pH value 10.3, and ammonia nitrogen value is
65ppm.The waste water composition be acetone 0.05%wt, hydrogen sulfide 10ppm, free ammonia 0.01%wt, dimethylamine 4ppm,
Yu Weishui.
It is detached using single column, pretreater 1, tower top control pressure 0.1MPa, 93.4 DEG C of tower top temperature, reflux ratio 1.3, tower
The whole extraction gas phases in top, form as acetone 31%wt, hydrogen sulfide 0.6%, dimethylamine 0.24%wt, ammonia 6.2%wt, remaining is
Vapor；COD value is 3 in tower reactor qualified water, and pH value 7.4, ammonia nitrogen value is 5ppm, meets industry water regeneration water quality standard
It is required that.
The embodiment wastewater treatment equipment is single column, for handling the taurine waste water of low ammonia nitrogen, low COD.
Embodiment 2
Taurine waste water (carries out the condensed water evaporated after desalting processing to produce with taurine using triple effect evaporation processing unit
The waste water that a large amount of waste water directly evaporated in the process obtain after merging)：COD value is 8920, pH value 10.3, and ammonia nitrogen value is
105ppm.The waste water composition be acetone 0.4%wt, hydrogen sulfide 10ppm, free ammonia 0.01%wt, dimethylamine 40ppm,
Remaining is water.
It is detached using single column, 1 tower top control pressure 0.15MPa of pretreater, 88.3 DEG C of tower top temperature, reflux ratio 2.4, tower
The whole extraction gas phases in top, form as hydrogen sulfide 3.6%, dimethylamine 4.8%wt, ammonia 15.1%wt, remaining is vapor.Side line
It produces as acetone 98.5%, remaining is water, COD value 9.3 in tower reactor qualified water, pH value 7.3, and ammonia nitrogen value 4.2ppm meets industry
The requirement of water reuse (treatment reuse water standard.
The embodiment wastewater treatment equipment is single column, for handling the taurine waste water of low ammonia nitrogen, high COD.
Embodiment 3
Taurine waste water (carries out the condensed water evaporated after desalting processing to produce with taurine using triple effect evaporation processing unit
The waste water that a large amount of waste water directly evaporated in the process obtain after merging)：COD value is 10362, pH value 11.4, and ammonia nitrogen value is
501ppm.The waste water composition is that acetone is 0.4%wt, hydrogen sulfide 200ppm, free ammonia 0.051%wt, and dimethylamine is
55ppm, remaining is water.
Using taurine wastewater zero discharge processing unit, 1 tower top control pressure 0.6MPa of pretreater, tower top temperature 7.4
DEG C, reflux ratio 1.8, the whole extraction gas phases of tower top are formed as hydrogen sulfide 28.2%, ammonia 71.8%wt, dimethylamine 100ppm,
Remaining is vapor.COD value is 9993 in tower reactor waste water, pH value 7.4, and ammonia nitrogen value is 3.7ppm.Acetone is in waste water at this time
In 1ppm hereinafter, dimethylamine is 620ppm, meeting industry water regeneration water quality standard will for 0.4%wt, hydrogen sulfide and ammonia content
It asks.
Top gaseous phase deammoniation treating column 7, the operating pressure of ammonia refining tower 7 is 0.5MPa, and operation temperature is 20 DEG C, saturated ammonia
It is 4.5L/Nm that water, which is recycled with the liquid-gas ratio of 1 tower top tail gas stream stock feed rate of pretreater,3(fluid flow/charging tail gas mark side
Number), the number of theoretical plate of ammonia refining tower 7 is 18 pieces, and saturation cyclic ammonia water feed entrance point is 3 pieces, and top is sealed using fresh ammonium hydroxide.
It is 15 DEG C that cooler 8, which controls cooling temperature, and the ammonia purity come out by ammonia refining tower 7 is in 99.6%wt, not sulfide hydrogen,
Yu Weishui.
1 tower reactor waste water of pretreater enters 12 tower top of rectifying column, control pressure 0.2MPa, and tower top temperature is 73.2 DEG C,
Reflux ratio is 0.6, and it is 98%wt that tower top fixed gas extraction gas phase, which is dimethyl ether, acetone 2%wt, liquid phase extraction acetone, purity
It is 99.5%, remaining is water.COD value is 1.2 in 12 tower reactor qualified water of rectifying column, pH value 7.2, and ammonia nitrogen value is 2.8ppm, is accorded with
Close the requirement of industry water regeneration water quality standard.
Note：Urban sewage reutilization water quality standard for industries (GB/T19923-2005), COD≤60, pH value≤
6.5-8.5 ammonia nitrogen value≤10ppm.
From above-described embodiment it is found that the COD value of the waste water obtained after above-mentioned treatment process and device, pH value, ammonia nitrogen value
Up to standard, all cycle water zero discharges, zero emission effectively by resource maximum utilizationization, reduce the pollution of environment simultaneously, should
With having a extensive future.
The above described is only a preferred embodiment of the present invention, not make limitation in any form to the present invention, though
So the present invention is disclosed above with preferred embodiment, however is not limited to the present invention, any technology people for being familiar with this profession
Member, without departing from the scope of the present invention, when the technology contents using the disclosure above make a little change or modification
For the equivalent embodiment of equivalent variations, as long as being the content without departing from technical solution of the present invention, technical spirit according to the present invention
To any simple modification, equivalent change and modification that above example is made, in the range of still falling within technical solution of the present invention.
Claims (10)
1. taurine waste water zero discharge treatment process, which is characterized in that include the following steps：
Taurine waste water is carried out desalting processing, removes salts substances therein, obtains desalination ox by step 1, desalting processing first
Sulfonic acid waste water；
The pretreatment of step 2, the desalination taurine waste water passes through the desalination taurine waste water obtained in the step 1
Reboiler（5）The pending substance of gas phase and the pending substance of liquid phase are formed after the vaporization process of part；
The reprocessing of step 3, the pending substance of the gas phase is passed through saturation ammonium hydroxide in the pending substance of gas phase, with the ox sulphur
Hydrogen sulfide in sour waste water reacts to form ammonium sulfate；
The reprocessing of step 4, the pending substance of the liquid phase, by the pending substance of the liquid phase in rectifying column（12）It is middle to carry out essence
It evaporates processing and isolates dimethylamine and acetone.
2. taurine waste water zero discharge treatment process according to claim 1, which is characterized in that used in the step 1
Triple effect evaporation or MVR evaporatings carry out desalting processing.
3. taurine waste water zero discharge treatment process according to claim 1, which is characterized in that locate in advance in the step 2
Reason is in pretreater（1）It carries out, and the pretreater（1）In operating pressure be 0.1-1.5MPa, reflux ratio 0.1-50,
Tower top operation temperature is 10-80 DEG C.
4. taurine waste water zero discharge treatment process according to claim 3, which is characterized in that the step 3 is in ammonia essence
Tower processed（7）Middle progress, and the ammonia refining tower（7）Operating pressure be equal to or less than the pretreater（1）Operating pressure,
Operation temperature is 5-50 DEG C.
5. taurine waste water zero discharge treatment process according to claim 1, which is characterized in that described in the step 3
The circulated sprinkling flow of saturation ammonium hydroxide is 1-10L/Nm with the liquid-gas ratio of the pending substance of the gas phase3。
6. taurine waste water zero discharge treatment process according to claim 1, which is characterized in that described in the step 4
Rectifying column（12）Tower top operating pressure be 0.1-0.4MPa, tower top temperature is 30-60 DEG C, reflux ratio 0.1-15.
7. taurine wastewater zero discharge processing unit, which is characterized in that including：
Pretreatment unit, including pretreater（1）, to it is described pretreatment provide heat reboiler（5）And it is arranged on described
Pretreater（1）The condensation reflux unit at top；
Gas-treatment means, including ammonia refining tower（7）, for passing through the pretreater（1）Treated, and gas phase is pending
Hydrogen sulfide reaction generation ammonium sulfate product in substance；
Liquid-phase treatment apparatus, including rectifying column（12）, with the pretreater（1）Outlet at bottom connects.
8. taurine wastewater zero discharge processing unit according to claim 7, which is characterized in that the condensation reflux unit
Including：
Pretreater condenser（2）, with the pretreater（1）Top exit connects, and passes through the pretreater for condensing
（1）The pending substance of gas phase that treated simultaneously generates liquid-phase reflux substance；
Pretreater return tank（3）, with the pretreater condenser（2）Connection, for recycling the liquid-phase reflux substance；
Pretreater reflux pump（4）, respectively with the pretreater return tank（3）, the pretreater（1）Connection, for inciting somebody to action
The pretreater is returned after the liquid-phase reflux substance supercharging（1）In.
9. taurine wastewater zero discharge processing unit according to claim 7, which is characterized in that the gas-treatment means
Further include ammonia refining cooler（10）, for the ammonia refining tower（7）Carry out cooling processing.
10. taurine wastewater zero discharge processing unit according to claim 7, which is characterized in that the liquid phase processing dress
It puts and further includes：
Rectifying column condenser（13）, it is arranged on the rectifying column（12）Tower top, for condensing the rectifying column（12）Overhead vapours；
Rectifying return tank（14）, with the rectifying column condenser（13）Connection passes through the rectifying column condenser for recycling
（13）Handle obtained liquid phase；
Rectifying reflux pump（15）, respectively with the rectifying return tank（14）, the rectifying column（12）Connection, for by the liquid phase
It is back to the rectifying column（12）In.
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Application publication date: 20180608 |