CN1293223A - Method for evaporating, concentrating and drying saponified waste alkali liquor - Google Patents
Method for evaporating, concentrating and drying saponified waste alkali liquor Download PDFInfo
- Publication number
- CN1293223A CN1293223A CN 99115602 CN99115602A CN1293223A CN 1293223 A CN1293223 A CN 1293223A CN 99115602 CN99115602 CN 99115602 CN 99115602 A CN99115602 A CN 99115602A CN 1293223 A CN1293223 A CN 1293223A
- Authority
- CN
- China
- Prior art keywords
- concentrating
- waste lye
- drying
- saponification waste
- saponification
- 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.)
- Granted
Links
- 239000002699 waste material Substances 0.000 title claims abstract description 88
- 238000000034 method Methods 0.000 title claims abstract description 35
- 238000001704 evaporation Methods 0.000 title claims abstract description 26
- 239000003513 alkali Substances 0.000 title claims abstract description 17
- 238000001035 drying Methods 0.000 title claims abstract description 14
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 23
- 230000008020 evaporation Effects 0.000 claims abstract description 14
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 12
- 238000001291 vacuum drying Methods 0.000 claims abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000011343 solid material Substances 0.000 claims abstract description 3
- 238000007127 saponification reaction Methods 0.000 claims description 68
- 238000010438 heat treatment Methods 0.000 claims description 13
- 239000007788 liquid Substances 0.000 claims description 13
- 238000005507 spraying Methods 0.000 claims description 11
- 238000007701 flash-distillation Methods 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 3
- 238000001694 spray drying Methods 0.000 claims description 3
- 241001253206 Andrias Species 0.000 claims 1
- 239000007921 spray Substances 0.000 abstract description 4
- 239000000463 material Substances 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 133
- 239000007787 solid Substances 0.000 description 10
- 239000000126 substance Substances 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 5
- 238000006386 neutralization reaction Methods 0.000 description 5
- 230000003647 oxidation Effects 0.000 description 5
- 238000007254 oxidation reaction Methods 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- 239000006200 vaporizer Substances 0.000 description 5
- 238000009833 condensation Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 239000012159 carrier gas Substances 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 239000000284 extract Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 150000007524 organic acids Chemical class 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- 230000008016 vaporization Effects 0.000 description 3
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Chemical compound CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- JHIVVAPYMSGYDF-UHFFFAOYSA-N cyclohexanone Chemical compound O=C1CCCCC1 JHIVVAPYMSGYDF-UHFFFAOYSA-N 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- FUZZWVXGSFPDMH-UHFFFAOYSA-N hexanoic acid Chemical compound CCCCCC(O)=O FUZZWVXGSFPDMH-UHFFFAOYSA-N 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- NQPDZGIKBAWPEJ-UHFFFAOYSA-N valeric acid Chemical compound CCCCC(O)=O NQPDZGIKBAWPEJ-UHFFFAOYSA-N 0.000 description 2
- 101100400452 Caenorhabditis elegans map-2 gene Proteins 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- AOWPVIWVMWUSBD-RNFRBKRXSA-N [(3r)-3-hydroxybutyl] (3r)-3-hydroxybutanoate Chemical class C[C@@H](O)CCOC(=O)C[C@@H](C)O AOWPVIWVMWUSBD-RNFRBKRXSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 235000019219 chocolate Nutrition 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- HPXRVTGHNJAIIH-UHFFFAOYSA-N cyclohexanol Chemical compound OC1CCCCC1 HPXRVTGHNJAIIH-UHFFFAOYSA-N 0.000 description 1
- 238000005202 decontamination Methods 0.000 description 1
- 230000003588 decontaminative effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 150000007520 diprotic acids Chemical class 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 230000035611 feeding Effects 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 150000002763 monocarboxylic acids Chemical class 0.000 description 1
- 239000012074 organic phase Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 235000017550 sodium carbonate Nutrition 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 238000013517 stratification Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000002076 thermal analysis method Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 229940005605 valeric acid Drugs 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Landscapes
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention relates to a method for evaporating, concentrating and drying saponified waste alkali liquor, which is characterized in that concentrated and separated saponified waste alkali liquor is heated by preheating equipment, mixed with nitrogen heated by water vapor and enters spray vacuum drying equipment for flash evaporation through atomizing equipment, and the saponified waste alkali liquor can be changed into solid material after being evaporated to dryness in a spray vacuum dryer. The method has the advantage of reducing the treatment cost such as material consumption, energy consumption and the like of the post-treatment of the saponified waste alkali liquor.
Description
The present invention relates to a kind of method of evaporating, concentrating and drying waste saponifying alkali solution.Saponification waste lye is that cyclohexane oxidation prepares in the pimelinketone process, with in the sodium hydroxide solution and the organic acid in the oxidation liquid, and the organic acid acetic in the saponification oxidation liquid and one waste liquid of obtaining.This waste liquid is a kind of chocolate strong basicity thick liquid, and chemical oxygen demand is up to hundreds thousand of.The saponification waste lye treatment process that adopts mainly contains burning method and reclaims organism method (being chemical method) with the acid neutralization both at home and abroad, and two kinds of methods respectively have characteristics.Burning method is decontamination more up hill and dale, by-product soda ash and steam.The organism method is reclaimed in the acid neutralization can recycle the multiple organic acid of deutero-(as butyric acid, valeric acid, caproic acid, hexanodioic acid) in the cyclohexane oxidation process, inorganic salt products such as recyclable sodium sulfate of while, produce the multiple fine chemical product that China market is in short supply, value added is high, certain potential economic benefit is arranged, realized turning waste into wealth.Producer adopts burning method to handle mostly at present.Before burning earlier will with saponification waste lye concentration from about the 28%wt through bringing up to about 45%wt after the evaporation concentration.Because the characteristic of saponification waste lye decision, evaporating concentration process is very easily fouling in interchanger, influence evaporation effect, total concentration admittedly is difficult to reach design load 50%wt, has strengthened the load of incinerator, expends heavy oil again, and owing to evaporate back phlegma band alkali contaminate environment again, therefore, improve total concentration admittedly, reducing the salkali waste total amount is to improve the effective way of treatment unit load.
The composition of the composition of saponification waste lye and characteristic saponification waste lye (saponification waste lye that concentrates back 42%wt at single vaporization is formed)
According to Institute of Chemistry, Academia Sinica's analytical results, its saponification waste lye classical group becomes organic monocarboxylic acid 10.89%wt, diprotic acid 1.36%wt, ketone ester compounds 4.24%wt, polymkeric substance 13.17%wt, Na (being converted into NaOH) 17.46%wt, water 52.88%wt.The characteristic parameter of saponification waste lye
By analyzing and testing, the composition of saponification waste lye and relevant physical data, the chemical oxygen demand of its saponification waste lye after single vaporization concentrates is 50-70 ten thousand mg/l, basicity is 13-19%wt, density 1.2-1.3g/cm
3, in the prior art, generally the viscosity when always being 50%wt admittedly for 111 ℃ is 7.641mPas, vapour pressure is 109.300Kpa, 30 ℃ of ctystallizing points.
Is 18%wt-31%wt from the cyclohexane oxidation high-tension unit without the general total solid content of spissated saponification waste lye, containing hexanaphthene during always admittedly for 18%wt is 0.02%wt, hexalin is 0.05%wt, pimelinketone is 0.11%wt, salt is 17.37%wt, and NaOH is 0.812%wt, and water is 79.43%wt, 96 ℃ of temperature, density 1174kg/m
3, viscosity 0.292mPas, vapour pressure 87.673Kpa, 1.0 ℃ of ctystallizing points.
As shown in Figure 1, send into saponification waste lye vaporizer 5 through saponification waste lye surge tank 1 back with saponification waste lye pump 4 without spissated saponification waste lye, through the step-down flash distillation, and evaporate with the 0.9Mpa steam heating, vapor-liquid separation in separator 6, saponification waste lye concentration rises to 41%wt-48%wt by 18%wt-31%wt, is sent to the incinerator processing through concentrating after saponification waste lye discharging pump 9.Gas phase enters condensate storage 8 alkane water stratifications after condenser 7 condensations, lower floor's water reclaims and does process water usefulness, and upper strata hexanaphthene organic phase is gone back to system and utilized.
From above-mentioned flow process, the saponification waste lye evaporative process is a simple flash distillation operation.Flow process is also uncomplicated, but control is difficult to stablize in actually operating, and fluctuation is big, is subject to disturb.It is to evaporate back phlegma band alkali and the serious impact biochemical treatment apparatus that this stage mainly shows, and causes the waste of process water and the increase of material consumption again owing to this strand phlegma can not get recycling.This problem is again because saponification waste lye instability of flow of the easy fouling of flash distillation and saponification waste lye charging in saponification waste lye vaporizer 5 causes, therefore, increased a saponification waste lye surge tank 1, by 4 feedings of saponification waste lye fresh feed pump, to stablize the saponification waste lye charging, lower cover at saponification waste lye vaporizer 5 has increased a coil pipe sparger again, feeds in the saponification waste lye vaporizer 5 as carrier gas with nitrogen, avoids saponification waste lye fouling in evaporative process.By above-mentioned two measures, stablized the saponification waste lye evaporation technology, eliminated evaporation back phlegma band alkali phenomenon, but total concentration admittedly of saponification waste lye is not improved.
Fig. 1 is among former saponification waste lye evaporation technology schematic flow sheet Fig. 1: 1-saponification waste lye surge tank 2-flash steam condenser
3-condensation liquid bath 4-saponification waste lye fresh feed pump
5-saponification waste lye vaporizer 6-separator
7-condenser 8-condensate storage
9-concentrates after saponification waste lye discharging pump 10-carrier gas line
11-goes incinerator conduit line map 2 among evaporating, concentrating and drying waste saponifying alkali solution process flow diagram Fig. 2 of the present invention: 1-saponification waste lye topping-up pump 2-saponification waste lye preheater
3-nitrogen preheater 4,5-atomizing nozzle
6-spraying vacuum drying device 7-condenser
8-water cooler 9-condensate storage
The 10-vacuum extracts device 11,12-high pressure steam line
13-saponification salkali waste solid material
The object of the present invention is to provide a kind of method of evaporating, concentrating and drying waste saponifying alkali solution.
Easily form the material of fouling at heating wall, when the main cause of its fouling is the solution evaporation It is overheated to be subjected to, or forms crystallization at heating wall gasification core place. By Thermal Analysis as can be known, exist When forming the nucleus of boiling on the general heating wall, wall is wanted overheated 3-5 ℃, and hence one can see that, solution The reason that has crystal to separate out during evaporation is the boiling vaporization owing to solution on the wall, at nucleus of boiling place Solution concentration improves suddenly, thereby crystallize out, and the crystal accumulation just forms fouling. Saponification waste lye is total The solid content height, easily fouling in evaporation process hinders heat transfer effect, causes heat exchange inhomogeneous. Logical Cross to the analysis of experiments of saponification waste lye as can be known, the evaporation of short of moisture, saponification waste lye is changing Less scaling in the hot device, and by experiment the proof, the saponification waste lye of 45%wt in the time of 1.0 ℃ also Non-crystallizable, just viscosity strengthens, and therefore, can conduct heat by forced turbulent under the supercharging, with the saponification salkali waste Liquid is heated into superheated liquid, sprays in the vacuum spray drying device by the air-flowing type sprayer then, very Under the dummy status, the moment flash distillation is with the moisture evaporate to dryness. Because spray-drying speed is fast, drying time is short, Generally only be 5-30s, and can directly obtain dry products, thereby can economize devaporation separation etc. Operation also can be continuously, automated production, stable operation, and operating environment is also better.
To (always admittedly be 25%wt～45%wt) with changing through the saponification waste lye of separator among Fig. 16 Saponification waste lye booster pump 1 after advancing is pressurized to that to send into saponification waste lye behind 2.0Mpa～2.5Mpa pre-In the hot device 2 with 3.0Mpa～4.0Mpa high pressure steam heating to 120 ℃～150 ℃, then with process Enter together mist with the 2.0Mpa of high pressure steam heating to 120 ℃～150 ℃～3.0Mpa high pressure nitrogen Change nozzle 4 and 5, atomized drop is controlled at 10 μ m～60 μ m, and is fast in spraying vacuum drying device 6 Speed flash steams, and the steam of flash distillation enters condensation in condenser 7, the cooler 8 by the top, and recycle-water can return Receive to utilize, fixed gas enters vacuum and extracts in the device 10 and vacuumize, and the General Proper reciprocal of duty cycle is-80Kpa～-90Kpa. In spraying vacuum drying device 6, can be changed into solid behind a large amount of evaporates to dryness of saponification waste lye moisture, Also can be by a control flash distillation amount simmer down to liquid, this will come according to the processing method of saponification waste lye Fixed, in general, adopt the chemical neutralization method saponification waste lye can be dried to solid particle, and adopt Burning rule should keep liquid.
The purpose of atomizer is by the atomizing of high pressure nitrogen spent lye to be sprayed into the very little drop of particle, is generally 10 μ m～60 μ m, provides very big evaporation surface, every m3The surface area that solution has is 100m2～600m
2, be beneficial to reach quick-drying purpose. Be conducive to spent lye Middle sodium salt separates with moisture, and the big I of drop is according to size and the needs of saponification waste lye flow The drying effect that reaches decides, can be for subsequent use with the spraynozzle of different size, and adopt hot nitrogen to do Be atomization gas, can be used as again hot carrier gas stream after making nitrogen in entering spray dryer steam is taken away. The spraying vacuum drying device should be beneficial to the timely evaporation of moisture, also is that vacuum is wanted height, is beneficial to again dried The sedimentation of the salkali waste particle after dry is because the extensive use of spraying vacuum drying technology and food, doctor During medicine, dyestuff etc. are produced, be comparatively ripe technology, so design selection is comparatively convenient. If Spent lye is dried to solid particle, also will considers to set up cyclone separator, increase feed bin and spiral transferring Send the solid transportation equipment such as machine.
Good effect of the present invention is:
If saponification waste lye is condensed into solid particle, will more be conducive to adopt chemical neutralization method place Manage this strand waste liquid, because this will reduce by 40%～50% sulfuric acid consumption, two of chemical neutralization method generation The amount of inferior waste water also will reduce 40%～50%, thus the real saponification waste lye of thoroughly processing. And if The employing burning method is processed, because the moisture in the saponification waste lye has reduced, also will greatly reduce fuel oil Consumption.
Embodiment 1:
To always for being pressurized to send in the saponification waste lye preheater 2 behind the 2.0Mpa with the saponification waste lye topping-up pump 1 after improving, the 25%wt saponification waste lye be heated to 150 ℃ admittedly with the 4.0Mpa high pressure steam, then with entering atomizing nozzle 4 and 5 through being heated to 150 ℃ 2.0Mpa high pressure chlorine with high pressure steam, atomizing droplet is controlled at 20 μ m, flash distillation rapidly in spraying vacuum drying device 6, the steam of flash distillation enters condenser 7 by the top, condensation in the water cooler 8, the recyclable utilization of recycle-water, non-condensable gas enters vacuum and extracts in the device 10 and vacuumize, and vacuum tightness is-90Kpa.In spraying vacuum drying device 6, can be changed into solid behind a large amount of evaporates to dryness of saponification waste lye moisture.
Embodiment 2:
Press of the saponification waste lye charging of the technology of embodiment 1 with 35%wt, be pressurized to 2.0Mpa, after being heated to 135 ℃, pressure with about 135 ℃ is that the high pressure nitrogen of 2.0Mpa enters atomizing nozzle, in vacuum tightness be-85Kpa about, when atomizing droplet is controlled at 40 μ m, in spraying vacuum drying device 6, can be changed into solid behind a large amount of evaporates to dryness of saponification waste lye moisture.
Embodiment 3:
Press of the saponification waste lye charging of the technology of embodiment 1 with 45%wt, be pressurized to 2.0Mpa, after being heated to 120 ℃, pressure with about 120 ℃ is that the high pressure nitrogen of 2.0Mpa enters atomizing nozzle, in vacuum tightness be-80Kpa about, when atomizing droplet is controlled at 60 μ m, in spraying vacuum drying device 6, can be changed into solid behind a large amount of evaporates to dryness of saponification waste lye moisture.
Claims (5)
1, a kind of method of evaporating, concentrating and drying waste saponifying alkali solution, with unconcentrated saponification waste lye through evaporation equipment step-down flash distillation, vapor-liquid separation behind the heating evaporation, improve the concentration of saponification waste lye, it is characterized in that the saponification waste lye after the concentrating and separating mixed and enter spraying vacuum drying equipment through atomising unit with nitrogen after the water steam-heated cal(l)andria after preliminary heating device heating carrying out flash distillation, in the spraying vacuum drying device, can be changed into the solid material behind a large amount of evaporates to dryness of saponification waste lye moisture.
2, according to the method for claims 1 described evaporating, concentrating and drying waste saponifying alkali solution, the Heating temperature that it is characterized in that saponification waste lye in preliminary heating device is 120 ℃～150 ℃.Pressure is 2.0Mpa～2.5Mpa.
3, according to the method for claims 1 described evaporating, concentrating and drying waste saponifying alkali solution, it is characterized in that employed nitrogen pressure is 2.0Mpa～3.0Mpa, the Heating temperature of nitrogen is in preliminary heating device: 120 ℃～150 ℃.
4, according to the method for claims 1 described evaporating, concentrating and drying waste saponifying alkali solution, the concentration range that it is characterized in that the charging saponification waste lye is 25%wt～45%wt.
5, according to the method for claims 1 described evaporating, concentrating and drying waste saponifying alkali solution, it is characterized in that in the spray drying device vacuum tightness for-80Kpa～-90Kpa.The atomizing droplet size of atomizing nozzle is 10 μ m～60 μ m.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99115602A CN1125863C (en) | 1999-10-18 | 1999-10-18 | Method for evaporating, concentrating and drying saponified waste alkali liquor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99115602A CN1125863C (en) | 1999-10-18 | 1999-10-18 | Method for evaporating, concentrating and drying saponified waste alkali liquor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1293223A true CN1293223A (en) | 2001-05-02 |
| CN1125863C CN1125863C (en) | 2003-10-29 |
Family
ID=5278537
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN99115602A Expired - Fee Related CN1125863C (en) | 1999-10-18 | 1999-10-18 | Method for evaporating, concentrating and drying saponified waste alkali liquor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1125863C (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102897963A (en) * | 2012-08-29 | 2013-01-30 | 赵志军 | Method for utilizing cyclohexanone waste alkali liquor as resource |
| CN109140463A (en) * | 2017-06-13 | 2019-01-04 | 中国石油化工股份有限公司 | A kind of method that cyclohexanone saponification waste lye burns |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5120989B1 (en) * | 1971-05-07 | 1976-06-29 | ||
| CN1010770B (en) * | 1988-08-29 | 1990-12-12 | 山西大学 | Preparation of soda using waste saponification liquor |
| CN1060758C (en) * | 1996-07-15 | 2001-01-17 | 巴陵石油化工公司鹰山石油化工厂 | Method for recovering useful substances from saponified waste alkali liquor |
-
1999
- 1999-10-18 CN CN99115602A patent/CN1125863C/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102897963A (en) * | 2012-08-29 | 2013-01-30 | 赵志军 | Method for utilizing cyclohexanone waste alkali liquor as resource |
| CN109140463A (en) * | 2017-06-13 | 2019-01-04 | 中国石油化工股份有限公司 | A kind of method that cyclohexanone saponification waste lye burns |
| CN109140463B (en) * | 2017-06-13 | 2020-12-18 | 中国石油化工股份有限公司 | Method for incinerating cyclohexanone saponification waste alkali liquor |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1125863C (en) | 2003-10-29 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2022051988A1 (en) | Method for preparing sucrose-6-ester | |
| CN101712521B (en) | Method for spraying and desalting through residual pressure of reverse osmosis concentrated water | |
| US11376521B2 (en) | Efficient distillation of ethanol | |
| CN109265314A (en) | The preparation method and preparation facilities of propylene glycol methyl ether acetate | |
| CN102211992A (en) | Process for reclaiming dibasic acid from adipic acid production waste solution | |
| CN109678820A (en) | A kind of method of complete thermal coupling abstraction distillation separation of tetrahydrofuran-ethyl alcohol-aqueous mixtures | |
| CN108939590A (en) | Energy-saving ethylene glycol rectification and purification equipment and technique | |
| CN202951265U (en) | Efficient evaporating crystallizer | |
| CN1125863C (en) | Method for evaporating, concentrating and drying saponified waste alkali liquor | |
| CN203196359U (en) | Outer circulating evaporator used to extract Chinese herbal medicines | |
| CN102321436B (en) | Resin short path distiller and resin distillation process | |
| CN115260028B (en) | Preparation and purification method of bio-based lubricating oil trimethylolpropane fatty acid triester | |
| CN104447216B (en) | A kind of beta naphthal continuous rectificating technique | |
| CN1188352C (en) | Waste alkali liquor oxidizing, decomposing, neutralizing and saponifying treatment with cyclohexane | |
| CN216472335U (en) | Energy-saving treatment device for steam condensate | |
| CN1049243C (en) | Process for removal of solvents from detergent pastes | |
| CN105858621A (en) | Method for concentrating titanium white waste acids through gas-liquid contact technology | |
| CN1301800A (en) | Process technology for mixed oil negative pressure evaporation | |
| CN209383430U (en) | Spent caustic treatment device in a kind of cyclohexanone preparation process | |
| CN102442884B (en) | Method for recovering ethanol during soy production process and device thereof | |
| CN205222912U (en) | Novel strong brine desalination equipment | |
| CN104829452A (en) | Energy-saving production system of ethyl acetate and corresponding energy-saving production technology | |
| CN217311990U (en) | Jet flash dryer and solvent removal system of surfactant | |
| WO2020019283A1 (en) | Propylene glycol methyl ether acetate rectification system and rectification method | |
| CN104671306A (en) | Waste treatment equipment for producing palm oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: CHINA PETROLEUM + CHEMICAL CORPORATION Free format text: FORMER OWNER: BALIN BRANCH CORP. SINOPEC Effective date: 20090605 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20090605 Address after: Chaoyang District, Chaoyangmen, North Street, No. 22, No. Patentee after: Sinopec Corp. Address before: Hunan province Yueyang Yingshan Petrochemical Factory Patentee before: Baling Branch, China Petro-Chemical Co., Ltd. |
|
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20031029 Termination date: 20171018 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |