CN102815812A - Optimization process method for recovering sodium sulfate form ethylene waste alkali - Google Patents
Optimization process method for recovering sodium sulfate form ethylene waste alkali Download PDFInfo
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- CN102815812A CN102815812A CN201110155499XA CN201110155499A CN102815812A CN 102815812 A CN102815812 A CN 102815812A CN 201110155499X A CN201110155499X A CN 201110155499XA CN 201110155499 A CN201110155499 A CN 201110155499A CN 102815812 A CN102815812 A CN 102815812A
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- oxidation
- waste lye
- ethylene waste
- neutralizer
- neutralization
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Links
- 239000002699 waste material Substances 0.000 title claims abstract description 67
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 60
- 239000005977 Ethylene Substances 0.000 title claims abstract description 58
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical group [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 title claims abstract description 42
- 238000000034 method Methods 0.000 title claims abstract description 41
- 238000005457 optimization Methods 0.000 title claims abstract description 8
- 239000003513 alkali Substances 0.000 title abstract description 6
- 238000006386 neutralization reaction Methods 0.000 claims abstract description 52
- 230000003647 oxidation Effects 0.000 claims abstract description 52
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 52
- 239000007788 liquid Substances 0.000 claims abstract description 44
- 238000009279 wet oxidation reaction Methods 0.000 claims abstract description 25
- 238000010790 dilution Methods 0.000 claims abstract description 22
- 239000012895 dilution Substances 0.000 claims abstract description 22
- 239000000243 solution Substances 0.000 claims abstract description 20
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 169
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 38
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 20
- 239000003795 chemical substances by application Substances 0.000 claims description 15
- 238000005189 flocculation Methods 0.000 claims description 15
- 230000016615 flocculation Effects 0.000 claims description 15
- HYHCSLBZRBJJCH-UHFFFAOYSA-M sodium hydrosulfide Chemical compound [Na+].[SH-] HYHCSLBZRBJJCH-UHFFFAOYSA-M 0.000 claims description 14
- 239000012535 impurity Substances 0.000 claims description 13
- 238000010907 mechanical stirring Methods 0.000 claims description 13
- 238000002156 mixing Methods 0.000 claims description 12
- 238000013022 venting Methods 0.000 claims description 12
- 230000005484 gravity Effects 0.000 claims description 10
- 235000017550 sodium carbonate Nutrition 0.000 claims description 9
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 9
- 230000001105 regulatory effect Effects 0.000 claims description 8
- 238000001035 drying Methods 0.000 claims description 7
- PANBYUAFMMOFOV-UHFFFAOYSA-N sodium;sulfuric acid Chemical compound [Na].OS(O)(=O)=O PANBYUAFMMOFOV-UHFFFAOYSA-N 0.000 claims description 7
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 6
- 229910001882 dioxygen Inorganic materials 0.000 claims description 6
- 230000001590 oxidative effect Effects 0.000 claims description 6
- 238000004062 sedimentation Methods 0.000 claims description 6
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 4
- 238000001704 evaporation Methods 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 4
- 238000001914 filtration Methods 0.000 claims description 4
- 238000003672 processing method Methods 0.000 claims description 4
- 238000012545 processing Methods 0.000 claims description 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 2
- 238000006243 chemical reaction Methods 0.000 claims description 2
- 238000002485 combustion reaction Methods 0.000 claims description 2
- 229920006395 saturated elastomer Polymers 0.000 claims description 2
- 238000005507 spraying Methods 0.000 claims description 2
- 229910021653 sulphate ion Inorganic materials 0.000 claims description 2
- 239000001117 sulphuric acid Substances 0.000 claims description 2
- 235000011149 sulphuric acid Nutrition 0.000 claims description 2
- 238000007738 vacuum evaporation Methods 0.000 claims description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 abstract description 10
- 235000011152 sodium sulphate Nutrition 0.000 abstract description 10
- 238000011084 recovery Methods 0.000 abstract description 4
- 239000000126 substance Substances 0.000 abstract description 3
- 238000000926 separation method Methods 0.000 abstract description 2
- 239000000706 filtrate Substances 0.000 abstract 2
- 229920002401 polyacrylamide Polymers 0.000 description 7
- 238000007865 diluting Methods 0.000 description 6
- 150000003839 salts Chemical class 0.000 description 6
- 239000011734 sodium Substances 0.000 description 6
- -1 mercaptan Chemical class 0.000 description 5
- 229910052751 metal Inorganic materials 0.000 description 5
- 239000002351 wastewater Substances 0.000 description 5
- 125000002091 cationic group Chemical group 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 229910052708 sodium Inorganic materials 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000007667 floating Methods 0.000 description 2
- 229910017053 inorganic salt Inorganic materials 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000002203 pretreatment Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 1
- 229910000287 alkaline earth metal oxide Inorganic materials 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 239000002781 deodorant agent Substances 0.000 description 1
- 238000004332 deodorization Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 150000004763 sulfides Chemical class 0.000 description 1
- 229910000314 transition metal oxide Inorganic materials 0.000 description 1
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- Removal Of Specific Substances (AREA)
Abstract
Disclosed is an optimization process method for recovering sodium sulfate form ethylene waste alkali. The method comprises that the ethylene waste alkali is subjected to wet oxidation and oxidation liquid is obtained; the oxidation liquid is subjected to first-step neutralization operation and an intermediate neutralization solution is obtained; the intermediate neutralization solution is subjected to separation and a clear solution or a filtrate is obtained; the clear solution or the filtrate is subjected to second-step neutralization operation and a neutralization solution is obtained; and the neutralization solution is dried and anhydrous sodium sulfate is obtained. By the aid of the method, the technical problems that the high salinity of the ethylene waste alkali which is subjected to the wet oxidation treatment, dilution and biochemical treatment can impact a biochemical treatment process is solved, the process is shortened, the investment for sodium sulfate recovery devices is reduced, and the method can be used in fields such as petrochemical industry, chemical industry, environment protection, comprehensive resource utilization and light industry.
Description
Technical field
The present invention relates to the wastewater from chemical industry recovery and utilization technology, be specifically related to a kind of method of comprehensive utilization of ethylene waste lye, particularly the optimization processing method of separating anhydrous sodium sulfate the ethylene waste lye after wet oxidation is handled, neutralized.
Background technology
Sour gas in the ethene cracking gas mainly comprises hydrogen sulfide, carbonic acid gas, organosulfur etc., for removing sour gas, takes the washing of alkaline solution and splitting gas counter current contact, and the waste liquid of generation is called ethylene waste lye.Remove in the waste lye and contain Na
2S, Na
2CO
3, NaOH and minor N a
2SO
3, Na
2S
2O
3Also contain organic sulfides such as mercaptan, thereby have unpleasant stink outward.
Methods such as biochemical treatment, comprehensive use were carried out in dilution after the method for improvement ethylene waste lye comprised direct facture, pre-treatment.Directly facture comprises deep-well injection, landfill, dilution discharge and burning, the use because environmental protection requirement has been under an embargo.The pre-treatment that ethylene waste lye is carried out comprises oxidation style or neutralisation, but pretreated ethylene waste lye contains a large amount of inorganic salt, directly enters composite wastewater treatment plant, will impact to biochemical treatment system, and causes the waste of inorganic salt.
The method forefathers of comprehensive utilization ethylene waste lye also have research.CN1789162 has proposed a kind of technique for reclaiming ethylene alkali-washing waste liquid, uses the transition metal oxide desulfurization behind the employing alkaline earth metal oxide causticization waste lye, and the sulfide that obtains is expected to become high value-added product, but does not have product to detect; It is the method for feedstock production S-WAT that CN1305954 has proposed with liquid hydrocarbon or waste alkali solution of gasoline, and the S-WAT of this method preparation still exists in solution, and contains more sodium sulfate impurity; CN101143293 has proposed a kind of method of deodorant waste lye absorbing treating smoke, and this method has produced the waste liquid that more contains high salt, and this method is used for the comprehensive utilization of the ethylene waste lye after the wet oxidation, is worth not as reclaim(ed) sulfuric acid sodium.
If the recovery of SODIUM SULPHATE ANHYDROUS 99PCT adopts oxidation-neutralization-crystallization-drying process to carry out in the ethylene waste lye, this process is used for the such recovery on a small scale of ethylene waste lye, and upward cost of investment is too high.
Summary of the invention
After the invention provides a kind of wet oxidation, neutralizing treatment ethylene waste lye, and the optimization processing method of reclaim(ed) sulfuric acid sodium therefrom are the optimization to " short flow and method ".Through the neutralization of two steps, can take out metals ion and carbonate step by step, thereby can under product condition up to standard, further reduce oxidation operation material, part are neutralized with the requirement of the quality of soda acid, reduce cost of investment; Can reduce salt amount after the optimization process to Waste Water Treatment and environmental emission; Reduce or avoid the impact of wet oxidation treat effluent and the follow-up biochemical treatment of contained high salt pair thereof; Also help ethylene production enterprise and carry out waste water recycling work, can be met the SODIUM SULPHATE ANHYDROUS 99PCT of the specification of quality of " GB/T6009-2003 industrial anhydrous sodium sulfate " without crystallization.
The method of reclaim(ed) sulfuric acid sodium specifically comprises following process in the ethylene waste lye of the present invention:
The method of reclaim(ed) sulfuric acid sodium comprises the steps: in a kind of ethylene waste lye
(1) ethylene waste lye is carried out wet oxidation and handle, wherein sulfide mainly is oxidized to vitriol, obtain oxidation liquid;
(2) oxidation liquid is carried out first step neutralization operation, neutralizer in the middle of obtaining;
(3) middle neutralizer is separated obtain clear liquid or filtrating
(4) clear liquid or filtrating are carried out second stage neutralization operation, obtain neutralizer;
(5) the neutralizer drying is obtained SODIUM SULPHATE ANHYDROUS 99PCT.
Described ethylene waste lye is through the ethylene waste lye of water or water vapour dilution, without in the ethylene waste lye of water or water vapour dilution any one; For selecting without the ethylene waste lye oxidation of water or water vapour dilution, neutralizer after the neutralization through water or water vapour dilution or without water or water vapour dilution.
In the step (1), sulfide mainly is oxidized to following method: the S of the main basis of judgement of vitriol
2-, S
2O
3 2-, SO
3 2-, SO
4 2-Can be by chemical analysis and ion-chromatographic determination, its measuring method is all with reference to GB; Can judge whether that through concentration ratio primary product is a vitriol.
Described ethylene waste lye is if the molar content ratio of Sodium sulfhydrate and yellow soda ash less than 1, directly carries out wet oxidation.
Described molar content ratio for Sodium sulfhydrate and yellow soda ash is greater than 1 ethylene waste lye; Complete oxidation can make its pH value be reduced to acidity; Receive the restriction of wet oxidation reaction equipment matter, rooting is regulated earlier the pH value of waste lye according to Sodium sulfhydrate content or is divided two-stage oxidizing and control the pH value of intermediate oxidation liquid according to Sodium sulfhydrate content possibly.
Described pH value of regulating waste lye according to Sodium sulfhydrate content earlier; Using massfraction in the step (1) earlier is that 30～45% sodium hydroxide solution is regulated molar content ratio that ethylene waste lye makes Sodium sulfhydrate and yellow soda ash in 0.95 to 1 scope, carries out wet oxidation again;
Described minute two-stage oxidizing and according to the pH value of Sodium sulfhydrate content control intermediate oxidation liquid, oxidation divides two sections in the step (1), and between the two-stage oxidizing reaction member, using massfraction is the pH value of 30～45% sodium hydroxide solution adjusting intermediate oxidation liquid; First section pH that is oxidizing to ethylene waste lye stopped wet oxidation at 4.3～7.5 o'clock, and using massfraction is that the pH value that 30～45% sodium hydroxide solution is regulated intermediate oxidation liquid is 8.8～10.5; And then carry out second section wet oxidation.
Described wet oxidation is treated to any one in wet type air oxide treatment or the processing of wet type dioxygen oxidation.
Described wet oxidation treatment temperature is 160 ℃～250 ℃; Pressure is to be higher than the saturated vapor pressure 20% of waste lye at each temperature; The residence time of wet oxidation reaction is different and change according to treatment temp, when being specially 160 ℃ of treatment temps, and the residence time >=5h; When treatment temp was 180 ℃, the residence time was >=3h; When treatment temp is 210 ℃, the residence time >=2h; When treatment temp is 250 ℃, the residence time >=1h; The residence time can infinitely prolong, but the sulphate content of oxidation liquid only can increase slightly, considers only to limit the minimum time that stops from economy.
It is described that to use sulphuric acid soln or the massfraction of mass percent concentration 70～98% for the ethylene waste lye after the oxidation be that 30～45% sodium hydroxide solution carries out neutralization reaction.
The neutralization reactor of the optional airtight normal pressure mechanical stirring of described neutralization reactor (if any the mechanical stirring neutralization reactor of venting port) or blast in the neutralization reactor of pneumatic blending any one.
In the step (2), first step neutralization operation, the neutralizer pH value that goes out reactor drum is controlled at 6.36～7.36, and metals ion is removed with sedimentary form, and carbonate is converted into supercarbonate, or part has become vitriol.
In the step (3), separation can be adopted sedimentation, filtration or air supporting to handle and remove impurity to neutralizer; Sedimentation can be adopted gravity settling or centrifugal settling; Sedimentation, filtration or air supporting are handled and can not added flocculation agent or add flocculation agent.
Said neutralizer is during without the dilution of water or water vapour, adopts when not adding the gravity settling of flocculation agent, and the required settling time is 16h to 48h.
Said neutralizer is when the dilution of water or water vapour, adopts the centrifugal settling that does not add flocculation agent, and the required settling time can be lower than neutralizer and adopt the gravity settling time that does not add flocculation agent for without water or water vapour dilution the time.
Said neutralizer is after water or water vapour dilution; Employing adds the gravity settling or the centrifugal settling of flocculation agent; The required settling time can be lower than neutralizer adopts the gravity settling time that does not add flocculation agent for without the dilution of water or water vapour the time, releases degree, flocculation agent kind dimly and confirms through experiment.
Said neutralizer comprises that through water or water vapour dilution ethylene waste lye is earlier through water or water vapour dilution; And then the neutralizer that obtains after the oxidation, neutralization, perhaps without the neutralizer that obtains after the ethylene waste lye oxidation of water or water vapour dilution, the neutralization any one in water or water vapour dilution again.
In the optional SEPIGEL 305 of said flocculation agent, the cationic-type polyacrylamide any one or multiple.
Said neutralizer does not add flocculation agent; Handle the product that can obtain meeting quality product requirement (specific targets " GB/T 6009-2003 industrial anhydrous sodium sulfate ") through air supporting, suitably use flocculation agent can make the quality product grade improve (such as bringing up to the II class) from the III class.
In the step (4), second stage neutralization operation, for the churned mechanically neutralization reactor of airtight normal pressure (if any the mechanical stirring neutralization reactor of venting port), the neutralizer pH value that goes out reactor drum is controlled at 4.36～5.36; For the neutralization reactor that blasts pneumatic blending, the neutralizer pH value that goes out reactor drum is controlled at 5.36～6.36, and supercarbonate is converted into vitriol and removes.
In the step (5), drying means can select that atmospheric evaporation is dry, vacuum-evaporation is dry, in the spraying drying any one; Or adopt the submerged combustion evaporation that lets flame contact saltcake liquid, obtain the SODIUM SULPHATE ANHYDROUS 99PCT product.
The invention has the beneficial effects as follows:
Through the neutralization of two steps, can remove metals ion and carbonate step by step, thereby can under product condition up to standard, further reduce oxidation operation material, part are neutralized with the requirement of the quality of soda acid, reduce cost of investment; Ethylene waste lye to after the deodorization is further handled; Reclaim(ed) sulfuric acid sodium; Can reduce salt amount to Sewage treatment systems and environmental emission; Reduce or avoid the impact of the follow-up biochemical treatment of high salt pair in the wet oxidation treat effluent, also help ethylene production enterprise and carry out other waste water recycling work.Through the optimal conditions of embodiment of the present invention, reduce approximately more than 90% to the salt amount of wastewater biochemical treatment facility and environmental emission, wastewater discharge reduces about more than 90%; Method such as need not burn can reach the specification of quality of " GB/T 6009-2003 industrial anhydrous sodium sulfate ".
Description of drawings
Fig. 1 is through the schematic flow sheet of the ethene alkali lye after 160 ℃～250 ℃ wet oxidations processing through neutralization, dried recovered SODIUM SULPHATE ANHYDROUS 99PCT.
Embodiment
Use the ethylene waste lye after certain enterprise's oil removing removes the gred to consist of (mass percent): NaOH 17.9%, Na among the embodiment 1-4
2S 3.8%, Na
2CO
31.7%, COD 25000mg/L, TOC 1300mg/L; Impurity metallic elements content is extremely low, Fe 0.6mg/L, Cr1.2mg/L, Ni 1.8mg/L, Cu 0.8mg/L, Ca, Mg (in Mg) 0.6mg/L, Cl 73.8mg/L.
Below in conjunction with accompanying drawing, specify through embodiment.
Embodiment 1
This ethylene waste lye is under the situation of not diluting with pH regulator, through 160 ℃ of (6MPa) wet type air oxidation 5h; Gained oxidation liquid uses mass concentration in the one-level neutralization reactor of drum pneumatic blending be that 98% the vitriol oil pH value that neutralizes is 7.09; In the middle of the gained neutralizer add SEPIGEL 305 (PAM) flocculation agent to 1ppm after filter and remove impurity; Filtrating in mechanical stirring, have that to continue to use mass concentration in the secondary neutralization reactor of venting port be that 98% the vitriol oil pH value that neutralizes is 4.53; The dry products therefrom sodium sulphate content of neutralizer is 98.93%, meets " GB-T 6009-2003 industrial anhydrous sodium sulfate " II class standard.
Embodiment 2
This ethylene waste lye is under the situation of not diluting with pH regulator, through 180 ℃ of (6MPa) wet type air oxidation 3h; Gained oxidation liquid uses mass concentration in the one-level neutralization reactor of drum pneumatic blending be that 98% the vitriol oil pH value that neutralizes is 7.31; Neutralizer gravity settling 36h removes impurity in the middle of the gained; Clear liquid continue to use mass concentration in the secondary neutralization reactor of drum pneumatic blending be that 98% the vitriol oil pH value that neutralizes is 5.43; The dry products therefrom sodium sulphate content of neutralizer is 98.26%, meets " GB-T 6009-2003 industrial anhydrous sodium sulfate " II class standard.
Embodiment 3
This ethylene waste lye is under the situation of not diluting with pH regulator, through 210 ℃ of (6MPa) wet type dioxygen oxidation 2h; Gained oxidation liquid in mechanical stirring, have that to use mass concentration in the one-level neutralization reactor of venting port be that 98% the vitriol oil pH value that neutralizes is 6.39; In the middle of the gained neutralizer add cationic polyacrylamide (CPAM) to the 0.3ppm gas through the floating impurity of removing; Clear liquid continue to use mass concentration in the secondary neutralization reactor of drum pneumatic blending be that 98% the vitriol oil pH value that neutralizes is 6.27; The dry products therefrom sodium sulphate content of neutralizer is 99.02%, meets " GB-T 6009-2003 industrial anhydrous sodium sulfate " I class standard.
Embodiment 4
This ethylene waste lye is under the situation of not diluting with pH regulator, through 240 ℃ of (6MPa) wet type dioxygen oxidation 1h; Gained oxidation liquid in mechanical stirring, have that to use mass concentration in the one-level neutralization reactor of venting port be that 70% the vitriol oil pH value that neutralizes is 6.83; Neutralizer adds cationic polyacrylamide (CPAM) and removes impurity through gravity settling 3h to 0.1ppm in the middle of the gained; Clear liquid in mechanical stirring, have that to use mass concentration in the secondary neutralization reactor of venting port be that 70% the vitriol oil pH value that neutralizes is 5.29; The dry products therefrom sodium sulphate content of neutralizer is 97.79%, meets " GB-T 6009-2003 industrial anhydrous sodium sulfate " II class standard.
Use the ethylene waste lye after certain enterprise's oil removing removes the gred to consist of (mass percent): NaOH 0% among the embodiment 5-8, NaHS 8.8%, Na
2CO
38.3%, COD 75000mg/L, TOC 2300mg/L; Impurity metallic elements content is extremely low, Fe 0.8mg/L, Cr 1.3mg/L, Ni 1.8mg/L, Cu 0.8mg/L, Ca, Mg (in Mg) 0.7mg/L, Cl 75.8mg/L.
Below in conjunction with accompanying drawing, specify through embodiment.
Embodiment 5
This ethylene waste lye is under the situation of not diluting with pH regulator; Through 160 ℃ of (6MPa) wet type air oxidation 2.5h; Gained intermediate oxidation liquid pH is 7.3, and using mass concentration is that the pH value that 30% sodium hydroxide is regulated intermediate oxidation liquid is 9.5, and continuation oxidation 2.5h gets oxidation liquid; Gained oxidation liquid uses mass concentration in the one-level neutralization reactor of drum pneumatic blending be that 98% the vitriol oil pH value that neutralizes is 7.08; In the middle of the gained neutralizer add SEPIGEL 305 (PAM) flocculation agent to 1ppm after filter and remove impurity; Filtrating in mechanical stirring, have that to continue to use mass concentration in the secondary neutralization reactor of venting port be that 98% the vitriol oil pH value that neutralizes is 4.53; The dry products therefrom sodium sulphate content of neutralizer is 98.95%, meets " GB-T6009-2003 industrial anhydrous sodium sulfate " II class standard.
Embodiment 6
This ethylene waste lye is under the situation of not diluting with pH regulator; Through 180 ℃ of (6MPa) wet type air oxidation 1.5h; Gained intermediate oxidation liquid pH is 6.3, and using mass concentration is that the pH value that 30% sodium hydroxide is regulated intermediate oxidation liquid is 10.5, and continuation oxidation 1.5h gets oxidation liquid; Gained oxidation liquid uses mass concentration in the one-level neutralization reactor of drum pneumatic blending be that 98% the vitriol oil pH value that neutralizes is 7.31; Neutralizer gravity settling 36h removes impurity in the middle of the gained; Clear liquid continue to use mass concentration in the secondary neutralization reactor of drum pneumatic blending be that 98% the vitriol oil pH value that neutralizes is 5.43; The dry products therefrom sodium sulphate content of neutralizer is 98.24%, meets " GB-T 6009-2003 industrial anhydrous sodium sulfate " II class standard.
Embodiment 7
This ethylene waste lye is 0.95: 1 with the molar content ratio that sodium hydroxide solution (massfraction is 30%) is adjusted to Sodium sulfhydrate and yellow soda ash; Employed mass concentration is that 30% sodium hydroxide solution quality is 11.0% of this ethylene waste lye quality, then through 210 ℃ of (6MPa) wet type dioxygen oxidation 2h; Gained oxidation liquid in mechanical stirring, have that to use mass concentration in the one-level neutralization reactor of venting port be that 98% the vitriol oil pH value that neutralizes is 6.40; In the middle of the gained neutralizer add cationic polyacrylamide (CPAM) to the 0.3ppm gas through the floating impurity of removing; Clear liquid continue to use mass concentration in the secondary neutralization reactor of drum pneumatic blending be that 98% the vitriol oil pH value that neutralizes is 6.27; The dry products therefrom sodium sulphate content of neutralizer is 99.01%, meets " GB-T 6009-2003 industrial anhydrous sodium sulfate " I class standard.
Embodiment 8
This ethylene waste lye is 0.98: 1 with the molar content ratio that sodium hydroxide solution (massfraction is 30%) is adjusted to Sodium sulfhydrate and yellow soda ash; Employed mass concentration is that 30% sodium hydroxide solution quality is 10.8% of this ethylene waste lye quality, then through 240 ℃ of (6MPa) wet type dioxygen oxidation 1h; Gained oxidation liquid in mechanical stirring, have that to use mass concentration in the one-level neutralization reactor of venting port be that 98% the vitriol oil pH value that neutralizes is 6.82; Neutralizer adds cationic polyacrylamide (CPAM) and removes impurity through gravity settling 3h to 0.1ppm in the middle of the gained; Clear liquid in mechanical stirring, have that to use mass concentration in the secondary neutralization reactor of venting port be that 98% the vitriol oil pH value that neutralizes is 5.28; The dry products therefrom sodium sulphate content of neutralizer is 97.73%, meets " GB-T 6009-2003 industrial anhydrous sodium sulfate " II class standard.
Claims (14)
1. the optimization processing method of a reclaim(ed) sulfuric acid sodium from ethylene waste lye is characterized in that comprising the steps:
(1) ethylene waste lye is carried out wet oxidation and handle, wherein sulfide mainly is oxidized to vitriol, obtain oxidation liquid;
(2) oxidation liquid is carried out first step neutralization operation, neutralizer in the middle of obtaining;
(3) middle neutralizer is separated obtain clear liquid or filtrating;
(4) clear liquid or filtrating are carried out second stage neutralization operation, obtain neutralizer;
(5) the neutralizer drying is obtained SODIUM SULPHATE ANHYDROUS 99PCT.
2. method according to claim 1 is characterized in that step (1) ethylene waste lye is for through the ethylene waste lye of water or water vapour dilution, without in the ethylene waste lye of water or water vapour dilution any one.
3. method according to claim 2 is characterized in that for the ethylene waste lye without the dilution of water or water vapour, and the neutralizer after oxidation, the neutralization can be selected through water or water vapour dilution or without water or water vapour dilution.
4. method according to claim 1 is characterized in that for the molar content ratio of Sodium sulfhydrate and yellow soda ash directly carrying out wet oxidation less than 1 ethylene waste lye.
5. method according to claim 1; It is characterized in that for the molar content ratio of Sodium sulfhydrate and yellow soda ash greater than 1 ethylene waste lye; Using massfraction in the step (1) earlier is that 30～45% sodium hydroxide solutions are regulated molar content ratio that ethylene waste lye makes Sodium sulfhydrate and yellow soda ash in 0.95 to 1 scope, carries out wet oxidation again.
6. method according to claim 1; It is characterized in that for the molar content ratio of Sodium sulfhydrate and yellow soda ash greater than 1 ethylene waste lye; Oxidation divides two sections in the step (1); Between the two-stage oxidizing reaction member, using massfraction is the pH value that 30～45% sodium hydroxide solutions are regulated intermediate oxidation liquid, and first section pH that is oxidizing to ethylene waste lye stopped wet oxidation at 4.3～7.5 o'clock, and using massfraction is that the pH value of 30～45% sodium hydroxide solutions adjusting intermediate oxidation liquid is 8.8～10.5; And then carry out second section wet oxidation.
7. according to claim 1,4,5,6 described arbitrary methods, it is characterized in that wet oxidation is treated to any one in wet type air oxide treatment or the processing of wet type dioxygen oxidation.
8. according to claim 1,4,5,6 described arbitrary methods, it is characterized in that the wet oxidation treatment temperature is 160 ℃～250 ℃; Pressure is to be higher than the saturated vapor pressure 20% of waste lye at each temperature; The residence time of wet oxidation reaction is different and change according to treatment temp, when being specially 160 ℃ of treatment temps, and the residence time >=5h; When treatment temp was 180 ℃, the residence time was >=3h; When treatment temp is 210 ℃, the residence time >=2h; When treatment temp is 250 ℃, the residence time >=1h; The residence time can infinitely prolong, but the sulphate content of oxidation liquid only can increase slightly, considers only to limit the minimum time that stops from economy.
9. according to claim 1,4,5,6 described arbitrary methods, it is characterized in that using the sulphuric acid soln or the mass percent concentration of mass percent concentration 70～98% for the ethylene waste lye after the oxidation is that 30～45% sodium hydroxide solutions carry out neutralization reaction.
10. method according to claim 1, it is characterized in that neutralization reactor is optional has the mechanical stirring neutralization reactor of venting port or blasts in the neutralization reactor of pneumatic blending any one.
11. method according to claim 1 is characterized in that step (2) first step neutralization operation, the neutralizer pH value that goes out reactor drum is controlled at 6.36～7.36.
12. method according to claim 1 is characterized in that step (3) is separated neutralizer can to adopt sedimentation, filtration or air supporting to handle to remove impurity; Sedimentation can be adopted gravity settling or centrifugal settling; Sedimentation, filtration or air supporting are handled and can not added flocculation agent or add flocculation agent.
13. method according to claim 1 is characterized in that step (4) second stage neutralization operation, for the mechanical stirring neutralization reactor that venting port is arranged, the neutralizer pH value that goes out reactor drum is controlled at 4.36～5.36; For the neutralization reactor that blasts pneumatic blending, the neutralizer pH value that goes out reactor drum is controlled at 5.36～6.36.
14. method according to claim 1 is characterized in that step (5) drying means can select that atmospheric evaporation is dry, vacuum-evaporation is dry, in the spraying drying any one; Or adopt the submerged combustion evaporation that lets flame contact saltcake liquid, obtain the SODIUM SULPHATE ANHYDROUS 99PCT product.
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| CN106587477A (en) * | 2016-12-21 | 2017-04-26 | 北京燕山翔宇环保工程技术有限公司 | System and method for treating industrial waste lye |
| CN112358079A (en) * | 2020-10-23 | 2021-02-12 | 锦州泰丰精细化工有限公司 | Regeneration process of sulfur-containing waste alkali liquor |
| CN118343935A (en) * | 2023-01-13 | 2024-07-16 | 中国石油化工股份有限公司 | Ethylene waste alkali liquid treatment method and device |
| CN118343937A (en) * | 2023-01-13 | 2024-07-16 | 中国石油化工股份有限公司 | A method and device for pretreating ethylene waste alkali liquid |
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| CN118343935A (en) * | 2023-01-13 | 2024-07-16 | 中国石油化工股份有限公司 | Ethylene waste alkali liquid treatment method and device |
| CN118343937A (en) * | 2023-01-13 | 2024-07-16 | 中国石油化工股份有限公司 | A method and device for pretreating ethylene waste alkali liquid |
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