CN111892523A - Method for removing acid and sodium by CHPPO device - Google Patents
Method for removing acid and sodium by CHPPO device Download PDFInfo
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- CN111892523A CN111892523A CN202010677180.2A CN202010677180A CN111892523A CN 111892523 A CN111892523 A CN 111892523A CN 202010677180 A CN202010677180 A CN 202010677180A CN 111892523 A CN111892523 A CN 111892523A
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- 238000000034 method Methods 0.000 title claims abstract description 99
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- 239000002253 acid Substances 0.000 title claims abstract description 18
- 239000011734 sodium Substances 0.000 title claims abstract description 18
- 229910052708 sodium Inorganic materials 0.000 title claims abstract description 18
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- 150000007524 organic acids Chemical class 0.000 claims abstract description 27
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical compound [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 claims abstract description 22
- 238000009776 industrial production Methods 0.000 claims abstract description 18
- 238000000926 separation method Methods 0.000 claims description 30
- FRIBMENBGGCKPD-UHFFFAOYSA-N 3-(2,3-dimethoxyphenyl)prop-2-enal Chemical compound COC1=CC=CC(C=CC=O)=C1OC FRIBMENBGGCKPD-UHFFFAOYSA-N 0.000 claims description 23
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 claims description 18
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- VFZRZRDOXPRTSC-UHFFFAOYSA-N DMBA Natural products COC1=CC(OC)=CC(C=O)=C1 VFZRZRDOXPRTSC-UHFFFAOYSA-N 0.000 claims description 4
- 238000009792 diffusion process Methods 0.000 claims description 3
- BDCFWIDZNLCTMF-UHFFFAOYSA-N 2-phenylpropan-2-ol Chemical compound CC(C)(O)C1=CC=CC=C1 BDCFWIDZNLCTMF-UHFFFAOYSA-N 0.000 claims description 2
- 238000006386 neutralization reaction Methods 0.000 claims description 2
- 239000006185 dispersion Substances 0.000 claims 1
- 238000011282 treatment Methods 0.000 abstract description 38
- 239000012071 phase Substances 0.000 description 81
- 238000005406 washing Methods 0.000 description 76
- 239000003921 oil Substances 0.000 description 52
- 230000001590 oxidative effect Effects 0.000 description 44
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 18
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 description 13
- 230000000694 effects Effects 0.000 description 12
- 239000000463 material Substances 0.000 description 10
- 239000003518 caustics Substances 0.000 description 8
- 239000008346 aqueous phase Substances 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 7
- 150000001299 aldehydes Chemical class 0.000 description 6
- 239000007795 chemical reaction product Substances 0.000 description 5
- 238000007599 discharging Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000003915 liquefied petroleum gas Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 238000003860 storage Methods 0.000 description 4
- DNIAPMSPPWPWGF-UHFFFAOYSA-N Propylene glycol Chemical compound CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000012544 monitoring process Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 3
- 239000011541 reaction mixture Substances 0.000 description 3
- 238000004062 sedimentation Methods 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 230000003068 static effect Effects 0.000 description 3
- JESIHYIJKKUWIS-UHFFFAOYSA-N 1-(4-Methylphenyl)ethanol Chemical compound CC(O)C1=CC=C(C)C=C1 JESIHYIJKKUWIS-UHFFFAOYSA-N 0.000 description 2
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000032798 delamination Effects 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000006735 epoxidation reaction Methods 0.000 description 2
- 238000011221 initial treatment Methods 0.000 description 2
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- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 238000007790 scraping Methods 0.000 description 2
- NWZSZGALRFJKBT-KNIFDHDWSA-N (2s)-2,6-diaminohexanoic acid;(2s)-2-hydroxybutanedioic acid Chemical compound OC(=O)[C@@H](O)CC(O)=O.NCCCC[C@H](N)C(O)=O NWZSZGALRFJKBT-KNIFDHDWSA-N 0.000 description 1
- JDSQBDGCMUXRBM-UHFFFAOYSA-N 2-[2-(2-butoxypropoxy)propoxy]propan-1-ol Chemical compound CCCCOC(C)COC(C)COC(C)CO JDSQBDGCMUXRBM-UHFFFAOYSA-N 0.000 description 1
- 239000004721 Polyphenylene oxide Substances 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- SZXQTJUDPRGNJN-UHFFFAOYSA-N dipropylene glycol Chemical compound OCCCOCCCO SZXQTJUDPRGNJN-UHFFFAOYSA-N 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- RTZKZFJDLAIYFH-UHFFFAOYSA-N ether Substances CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 1
- 239000003063 flame retardant Substances 0.000 description 1
- IKDUDTNKRLTJSI-UHFFFAOYSA-N hydrazine monohydrate Substances O.NN IKDUDTNKRLTJSI-UHFFFAOYSA-N 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 239000003999 initiator Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 229920000570 polyether Polymers 0.000 description 1
- 229920005862 polyol Polymers 0.000 description 1
- 150000003077 polyols Chemical class 0.000 description 1
- 239000004814 polyurethane Substances 0.000 description 1
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- 238000002360 preparation method Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- RUOJZAUFBMNUDX-UHFFFAOYSA-N propylene carbonate Chemical compound CC1COC(=O)O1 RUOJZAUFBMNUDX-UHFFFAOYSA-N 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
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- 229920006305 unsaturated polyester Polymers 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C407/00—Preparation of peroxy compounds
- C07C407/003—Separation; Purification; Stabilisation; Use of additives
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Epoxy Compounds (AREA)
Abstract
The invention relates to a method for separating, removing acid and sodium by a CHPPO device, which mainly solves the problems of undefined process, imperfect flow, large equipment investment and high operation cost in the prior art. By adopting the method, a mixer, a centrifuge and an oil-water device are arranged in a CHPPO device of 5-80 ten thousand tons/year, a centrifuge oil phase is set to contain a small amount of water phase, and a centrifuge water phase does not contain the oil phase; the impurity-containing oxidation liquid is subjected to acid and sodium removal treatment to obtain purified oxidation liquid with organic acid impurities of less than or equal to 50mg/kg and sodium ion impurities of less than or equal to 1.0mg/kg, the equipment investment is saved by 65.89-68.62%, the operation cost is saved by 7.74-11.73%, the problems are well solved, and the method can be applied to PO industrial production of CHPPO devices.
Description
Technical Field
The invention relates to the technical field of propylene oxide, in particular to a method for removing organic acid impurities and sodium ion impurities in cumene hydroperoxide oxidizing liquid of a CHPPO device by adopting a mixer combined with a centrifuge and an oil-water separator.
Background
Propylene oxide is an important chemical raw material and is also one of three large derivatives of propylene. The method is mainly used for producing polyether polyol, polyurethane, propylene glycol, unsaturated polyester, propylene glycol ether, dipropylene glycol ether, flame retardants, synthetic lubricating oil, surfactants, propylene carbonate and the like, and the application field of the method is spread in the aspects of chemical basic industry and daily life of people.
The technology of the CHPPO method for preparing the propylene oxide by the cumene oxidation has the characteristics of less three-waste discharge, no coproduct, high safety and environmental protection, and is one of the most promising technologies for preparing the propylene oxide in the future. The main process of the CHPPO method comprises the following steps: cumene hydroperoxide CHP is generated by oxidizing cumene hydroperoxide, the cumene hydroperoxide CHP is used as an oxidizing agent to perform epoxidation reaction with propylene to generate epoxypropane PO and dimethyl benzyl alcohol DMBA epoxidation reaction products, and the reaction products are separated and refined to generate high-quality epoxypropane PO products; the dimethyl benzyl alcohol DMBA is hydrogenolyzed to generate cumene, and the cumene is oxidized into cumene hydroperoxide CHP for recycling.
The invention patent application number in the prior art is CN201611168755.8 a method and a device for preparing cumene hydroperoxide by oxidizing cumene, which discloses that in a first microreactor group formed by connecting one or more microreactors in series, the cumene and an initiator are introduced into a first microreactor in the first microreactor group, a reaction product obtained after the oxidation reaction flows into a second microreactor in the first microreactor group for oxidation reaction, continuous flow type oxidation reaction is carried out in sequence by recursion until the reaction product finally flows into a last microreactor for oxidation reaction, and the reaction product is finally purified; in each oxidation reaction process, oxygen is introduced into all the microreactors, and the molar ratio of the cumene introduced into the first microreactor to the sum of the oxygen introduced into all the microreactors is 0.1: 5. the invention solves the problems of large reaction temperature fluctuation, low production efficiency and low yield of the traditional process. The invention discloses a method for removing aldehydes in a propylene oxide reaction mixture with patent application number CN201610115263.6, which comprises the following steps: the reaction mixture of the propylene oxide is primarily dealdehydized through a dealdehyding resin tank, so that the aldehyde content is reduced, and the product purity of the propylene oxide is ensured; sequentially removing water and unreacted propylene, feeding the material containing propylene oxide and methanol into a propylene oxide refining tower, extracting the methanol by using desalted water containing ethanolamine or hydrazine hydrate at the middle section of the tower, and removing residual aldehyde in a propylene oxide product; the separated water solution is separated by a methanol tower and then enters a membrane separation facility to further remove residual aldehyde and impurities, the methanol at the permeation side returns to the reaction system to be used as circulating methanol, and the methanol containing aldehyde at the permeation side returns to a collection tank. The method has the advantages of less equipment and reduced one-time investment; the separation and recovery process does not need to introduce hydrogen, does not increase safety risk, is safe and reliable to use, and can reduce the energy consumption of subsequent wastewater treatment. The invention has the technical scheme that the static mixer comprises a pipe body, wherein spiral plates are coaxially and fixedly connected in the pipe body and are divided into a left spiral plate and a right spiral plate, the left spiral plate and the right spiral plate are sequentially and alternately arranged, the adjacent left spiral plate and the adjacent right spiral plate are alternately and fixedly connected, the adjacent side walls, close to each other, of the left spiral plate and the adjacent right spiral plate are vertically arranged, and a plurality of turbulence rods vertical to the curved surface of the left spiral plate or the right spiral plate are fixedly connected in the pipe body; therefore, the mixing effect of the mixer is improved. The invention discloses a high-speed sedimentation separation device with the patent application number of CN201810804726.9, which comprises an outer cylinder body, a first-layer sleeve, a second-layer sleeve, a third-layer sleeve, a bottom mud scraping assembly, a transmission connecting part, a power driving device and a top mud scraping assembly, wherein the first-layer sleeve, the second-layer sleeve and the third-layer sleeve are sequentially sleeved in the outer cylinder body from inside to outside, the opening of the first-layer sleeve is upward, the upper end and the lower end of the second-layer sleeve are respectively provided with an opening communicated with the inner cavity of the second-layer sleeve, and. The invention can make sewage slowly flow into the outer cylinder body by arranging the three layers of sleeves sleeved from inside to outside in sequence in the outer cylinder body, the water flow speed is slow, the static settlement separation can be simulated to a greater extent, meanwhile, the water flow path can be prolonged, the reaction is fully realized, the sedimentation separation effect is good, the top blowdown overflow, the bottom blowdown backwashing and the middle and upper clear water discharge can be synchronously realized, and the continuous operation of the system can be ensured without standing and waiting. The invention patent application number is CN201911118686.3 centrifugal separation device, includes: a tank body; a filter cartridge; a bearing seat; a gear case; a second motor; a screw assembly; a first drive assembly; and (4) feeding a pipe. The centrifugal separation device provided by the invention adopts the mode that the filter cartridge is matched with the spiral for solid-liquid separation, the whole occupied area is small, the large diameter of the spiral is closer to the inner diameter of the filter cartridge, and the accumulation of filter residues is not easy to generate. The invention has the patent application number of CN201910915370.0 and comprises a middle storage tank, a primary treatment tank and a secondary treatment tank, wherein the middle storage tank is connected with the secondary treatment tank through a connecting pipe, the lower part of the middle storage tank is provided with a sediment discharge port, the upper part of the middle storage tank is provided with an electric power system and a monitoring system, the upper part of the primary treatment tank is provided with an oil outlet and a medium inlet, the lower end of the medium inlet is connected with an oil pump, the upper part of the oil outlet is provided with a compressed air valve, the lower part of the oil outlet is provided with an; the upper part of the secondary treatment tank is provided with an oil discharge arch valve, an oil outlet, a compressed air valve and a monitoring system, the compressed air valve is positioned at the upper end of the oil outlet, the oil discharge arch valve and the monitoring system are arranged in the middle, the lower part of the secondary treatment tank is provided with a water outlet, a sewage circulation port, a medium return port and a drain valve, and the water outlet is positioned at the lower end of the secondary treatment tank; therefore, the invention has the advantages of large sewage treatment capacity, good treatment effect, high oil-water separation efficiency and wide application prospect. The invention discloses alkaline washing desulfurization equipment for liquefied petroleum gas, which has a patent application number of CN201920187241.X and relates to the technical field of alkaline washing desulfurization of liquefied petroleum gas.
The invention discloses a method and a device for preparing cumene hydroperoxide by oxidizing cumene, which belongs to the prior art and is provided with a patent application number of CN201611168755.8, and a method for removing aldehydes in epoxypropane reaction mixture, which is provided with a patent application number of CN201610115263.6, only discloses a preparation process of the cumene hydroperoxide, and does not relate to a method for removing organic acid impurities and sodium ion impurities in cumene hydroperoxide oxidizing liquid of a CHPPO device. The invention relates to a static mixer with patent application number of CN201910976504.X, a high-speed sedimentation separation device with patent application number of CN201810804726.9, a centrifugal separation device with patent application number of CN201911118686.3 and an oil-water separator with patent application number of CN201910915370.0, which only disclose the operation function of a single device and do not relate to a means for connecting the mixer, the centrifugal device and the oil-water separator in a process flow to remove organic acid impurities and sodium ion impurities in cumene hydroperoxide oxidizing liquid of a CHPPO device. The invention discloses alkali washing and desulfurizing equipment for liquefied petroleum gas with the patent application number of CN201920187241.X, and only discloses a method for treating liquefied petroleum gas by adopting an alkali washing tower/water washing tower with large equipment engineering investment and high operation cost. Therefore, in the prior art, the problems of unclear process technology, imperfect process flow, large investment in equipment engineering and high operation and running cost exist in the process of purifying the cumene hydroperoxide oxidizing solution by the CHPPO device.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides a method for removing acid and sodium from a CHPPO device, so that the process technology is further defined, the process flow is improved, the equipment engineering investment is reduced, and the operation cost is reduced.
In order to achieve the purpose, the invention adopts the following technical scheme:
the invention provides a method for separating, removing acid and sodium from a CHPPO device, which comprises the following process flows in a large-scale commercial CHPPO industrial production device with nominal capacity of 5-80 ten thousand tons per year:
mixing a heterooxidation liquid containing cumene hydroperoxide containing organic acid impurities and sodium ion impurities from outside with a pressurized water phase of a delayer, entering the first mixer, entering a fresh alkali liquor from outside into the first mixer, discharging the mixed first mixer, entering a first centrifuge, performing centrifugal separation, entering an oil phase of the first centrifuge which flows out into an oil-water delayer, performing oil-water demixing, entering an oil phase of the delayer which flows out into a second mixer, also entering fresh water from outside into the second mixer, discharging the mixed second mixer, entering a second centrifuge, performing centrifugal separation, entering an oil phase of the second centrifuge which flows out into the oil-water separator, performing oil-water separation, and sending the oil phase of the separator which flows out to outside as a purified oxidation liquid of the cumene hydroperoxide containing no organic acid impurities and sodium ion impurities;
the water phase of the first centrifuge flowing out of the first centrifuge enters an oil-water demixer and is subjected to oil-water demixing, and the water phase of the flowing-out demixer is pressurized by a water phase pump of the demixer and then is combined with the mixed oxidation liquid coming from the outside to enter a first mixer; the effluent waste alkali liquor is sent out;
and the water phase of the second centrifuge flowing out of the second centrifuge enters an oil-water separator, and is subjected to oil-water separation, and the water phase of the outflow separator is taken as wastewater to be discharged outside.
Furthermore, the mixed oxidation liquid containing organic acid impurities and sodium ion impurities from the outside flows and is divided, liquid drops are dispersed, liquid-liquid contact, radial mixing, blending diffusion and oil-water combination are carried out in a first mixer, and the organic acid impurities in the mixed oxidation liquid and the fresh alkali liquor are subjected to neutralization reaction and are removed;
the oil phase and the water phase with different densities are gathered and separated by using the centrifugal force generated in the rotating process of the first centrifuge, the oil phase of the first centrifuge flowing out from the inner edge of the first centrifuge is allowed to contain a small amount of water phase, and the water phase of the first centrifuge flowing out from the outer edge of the first centrifuge is not allowed to contain oil phase;
the first centrifuge oil phase and the first centrifuge water phase respectively enter different parts of the oil-water delaminator, and the delaminator oil phase without the water phase flows out of the top of the oil-water delaminator;
the method comprises the following steps of flowing and dividing a delaminator oil phase containing sodium ion impurities and fresh water in a second mixer, dispersing liquid drops, contacting liquid and liquid, radially mixing, mixing and diffusing, and combining oil and water, wherein the sodium ion impurities in the delaminator oil phase are dissolved and removed by the fresh water;
the oil phase and the water phase with different densities are gathered and separated by using the centrifugal force generated in the rotating process of the second centrifuge, the oil phase of the second centrifuge flowing out from the inner edge of the second centrifuge is allowed to contain a small amount of water phase, and the water phase of the second centrifuge flowing out from the outer edge of the second centrifuge is not allowed to contain oil phase;
the oil phase of the second centrifuge and the water phase of the second centrifuge respectively enter different parts of the oil-water separator, and the oil phase of the delaminator which flows out from the top of the oil-water separator and does not contain the water phase is taken as purified oxidation liquid to be sent out.
Further, the first centrifuge oil phase and the first centrifuge water phase respectively enter different parts of the oil-water delaminator; the oil-water demixer top flows out of the oil phase of the demixer without the water phase.
Further, the oil phase of the second centrifuge and the water phase of the second centrifuge respectively enter different parts of the oil-water separator; the oil phase of the separator flowing out of the top of the oil-water separator does not contain the aqueous phase.
Furthermore, the heterooxidation liquid contains 51.7 to 77.3 weight percent of cumene, 20.0 to 38.0 weight percent of cumene hydroperoxide CHP, 2.0 to 9.0 weight percent of alpha, alpha-dimethyl benzyl alcohol DMBA, 0.4 to 0.7 weight percent of light component, 0.3 to 0.6 weight percent of heavy component, 1000mg/kg of organic acid and 40 to 160mg/kg of sodium ion.
Further, the first mixer is operated at a pressure of 0.45-1.05MPaA and at a temperature of 25-85 ℃; the operating pressure of the first centrifuge is 0.40-1.00MPaA, and the operating temperature is 25-85 ℃; the operation pressure of the inlet of the water phase pump of the delaminator is 0.40-1.00MPaA, the operation pressure of the outlet is 0.55-1.15MPaA, and the operation temperature is 25-85 ℃; the operating pressure of the oil-water separator is 0.38-0.98MPaA, and the operating temperature is 25-85 ℃.
Further preferably, the first mixer is operated at a pressure of 0.55 to 0.95MPaA and at a temperature of 35 to 75 ℃; the operating pressure of the first centrifuge is 0.50-0.90MPaA, and the operating temperature is 35-75 ℃; the operation pressure of the inlet of the water phase pump of the delayer is 0.50-0.90MPaA, the operation pressure of the outlet is 0.65-1.05MPaA, and the operation temperature is 35-75 ℃; the operating pressure of the oil-water separator is 0.48-0.88MPaA, and the operating temperature is 35-75 ℃.
More preferably, the first mixer is operated at a pressure of 0.65 to 0.85MPaA and at a temperature of 45 to 65 ℃; the operating pressure of the first centrifuge is 0.60-0.80MPaA, and the operating temperature is 45-65 ℃; the operation pressure of the inlet of the water phase pump of the delayer is 0.60-0.80MPaA, the operation pressure of the outlet is 0.75-0.95MPaA, and the operation temperature is 45-65 ℃; the operating pressure of the oil-water separator is 0.58-0.78MPaA, and the operating temperature is 45-65 ℃.
Further, the second mixer is operated at a pressure of 0.35-0.95MPaA and at a temperature of 25-85 ℃; the operating pressure of the second centrifuge is 0.30-0.90MPaA, and the operating temperature is 25-85 ℃; the oil-water separator has an operating pressure of 0.28-0.88MPaA and an operating temperature of 25-85 ℃.
Further preferably, the second mixer is operated at a pressure of 0.45 to 0.85MPaA and at a temperature of 35 to 75 ℃; the operating pressure of the second centrifuge is 0.40-0.80MPaA, and the operating temperature is 35-75 ℃; the oil-water separator has an operating pressure of 0.38-0.78MPaA and an operating temperature of 35-75 ℃.
More preferably, the second mixer is operated at a pressure of 0.55 to 0.75MPaA and at a temperature of 45 to 65 ℃; the operating pressure of the second centrifuge is 0.50-0.70MPaA, and the operating temperature is 45-65 ℃; the operating pressure of the oil-water separator is 0.48-0.68MPaA, and the operating temperature is 45-65 ℃.
By adopting the technical scheme, compared with the prior art, the invention has the following technical effects:
the invention relates to a method for separating, removing acid and sodium from a CHPPO device, which is characterized in that for a large-scale commercial CHPPO industrial production device with nominal capacity of 5-80 ten thousand tons/year, a 'first mixer-first centrifuge-oil-water demixer' alkaline washing process flow and a 'second mixer-second centrifuge-oil-water separator' water washing process flow are adopted to replace the 'alkaline washing tower-water washing tower' process flow in the prior art, a centrifuge oil phase is set to contain a small amount of water phase, and a centrifuge water phase is not allowed to contain an oil phase; the cumene hydroperoxide impurity oxidation liquid containing 200-1000mg/kg organic acid impurities and 40-160mg/kg sodium ion impurities is subjected to acid removal and sodium removal treatment to obtain the cumene hydroperoxide purified oxidation liquid with the organic acid impurity content of less than or equal to 50mg/kg and the sodium ion impurity content of less than or equal to 1.0mg/kg, so that the investment of equipment engineering can be saved by 65.89-68.62%, the operation cost can be saved by 7.74-11.73%, and a better technical effect is achieved.
Drawings
FIG. 1 is a schematic process flow diagram of the present invention;
wherein, 11-a first mixer, 12-a delayer water phase pump, 13-a first centrifuge, 14-an oil-water delayer, 15-a second mixer, 16-a second centrifuge, 17-an oil-water separator, A1-a miscellaneous oxidizing liquid, A2-a purified oxidizing liquid, A3-a first mixer discharge, A4-a first centrifuge oil phase, A5-a delayer oil phase, A6-a second mixer discharge, A7-a second centrifuge oil phase, B1-fresh lye, B2-waste lye, B3-a first centrifuge water phase, B4-a delayer water phase, C1-fresh water, C2-waste water, C3-a second centrifuge water phase;
the process flow of the invention is described as follows:
the impurity-containing oxidation liquid A1 of cumene hydroperoxide containing organic acid impurities and sodium ion impurities from the outside is combined with a pressurized water phase B4 of a delayer and enters a first mixer 11, a fresh lye B1 from the outside also enters the first mixer 11, a mixed discharge A3 of the first mixer enters a first centrifuge 13, the first centrifuge oil phase A4 which flows out after centrifugal separation enters an oil-water delayer 14 and is subjected to oil-water delamination, an effluent oil phase A5 of the delayer enters a second mixer 15, a fresh water C1 from the outside also enters the second mixer 15, a mixed discharge A6 of the second mixer enters a second centrifuge 16 and is subjected to centrifugal separation, an effluent oil phase A7 of the second centrifuge enters an oil-water separator 17, the oil-water separation is carried out, and an effluent oil phase is taken as a purified oxidation liquid A2 of the cumene hydroperoxide containing no organic acid impurities and sodium ion impurities and is sent out of the outside. The water phase B3 of the first centrifuge flowing out of the first centrifuge enters an oil-water demixer 14 for oil-water demixing, and the water phase B4 of the flowing-out demixer is pressurized by a demixer water phase pump 12 and then is combined with the mixed oxidation liquid A1 from the outside to enter a first mixer 11; the effluent waste lye B2 is discharged outside. The second centrifuge aqueous phase C3 flowing out of the second centrifuge enters the oil-water separator 17, is subjected to oil-water separation, and the outflow separator aqueous phase is sent out as wastewater C2.
FIG. 2 is a schematic process flow diagram of the prior art;
1-an alkaline washing tower, 2-a circulating lye pump, 3-an alkaline washing tower kettle pump, 14-an oil-water demixer, 5-a water washing tower, 6-a water washing tower kettle pump, 17-an oil-water separator, A1-a miscellaneous oxidizing liquid, A2-a purified oxidizing liquid, A8-an alkaline washing tower top discharge, A5-a demixer oil phase, A9-a separator oil phase, B1-a fresh alkali liquid, B2-a waste alkali liquid, B5-a circulating alkali liquid, B6-an alkaline washing tower kettle discharge, C1-fresh water, C2-waste water and C4-a water washing tower kettle discharge.
The process flow of the prior art is described as follows:
mixing impurity-containing oxidation liquid A1 from the outside with oil phase A5 of a demixer, feeding the mixture into the tower kettle of an alkaline washing tower 1, mixing fresh alkaline liquor B1 from the outside with circulating alkaline liquor B5, feeding the mixture into the tower top of the alkaline washing tower 1, performing alkaline washing, mixing alkaline washing tower top discharge A8 flowing out from the tower top of the alkaline washing tower with oil phase A9 of a separator, feeding fresh water C1 from the outside into the tower top of a water washing tower 5, performing water washing, and feeding purified oxidation liquid A2 flowing out from the tower top of the water washing tower out of the outside. Circulating alkali liquor B5 flowing out of the tower kettle of the alkaline washing tower is pressurized by a circulating alkali liquor pump 2 and returns to the top of the alkaline washing tower 1, discharging liquid B6 flowing out of the tower kettle of the alkaline washing tower enters an oil-water delayer 14 by pressurization of an alkaline washing tower kettle pump 3, oil-water demixing is carried out, an oil phase A5 flowing out of the delayer is merged with a mixed oxidizing liquid A1 and enters the tower kettle of the alkaline washing tower 1, and an aqueous phase flowing out of the delayer is sent out of the office as waste alkali liquor B2. The effluent C4 from the bottom of the water washing tower enters an oil-water separator 17 through the pressurization of a water washing tower bottom pump 6, the oil phase A9 of the effluent separator and the effluent A8 from the top of the alkaline washing tower are combined and enter the bottom of a water washing tower 5 through oil-water separation, and the water phase of the effluent separator is taken as wastewater C2 and is sent out.
Detailed Description
The invention provides a method for removing acid and sodium by a CHPPO device. The present invention will be described in detail and specifically with reference to the following examples to facilitate better understanding of the present invention, but the following examples do not limit the scope of the present invention.
Comparative example 1
Taking a commercial CHPPO industrial production device with nominal capacity of 5 ten thousand tons/year as an example, as shown in fig. 2, the prior art adopts a process flow of 'caustic wash tower-water wash tower' to treat the oxidation liquid containing impurities, and the specific contents comprise the following: mixing impurity-containing oxidation liquid A1 from the outside with oil phase A5 of a demixer, feeding the mixture into the tower kettle of an alkaline washing tower 1, mixing fresh alkaline liquor B1 from the outside with circulating alkaline liquor B5, feeding the mixture into the tower top of the alkaline washing tower 1, performing alkaline washing, mixing alkaline washing tower top discharge A8 flowing out from the tower top of the alkaline washing tower with oil phase A9 of a separator, feeding fresh water C1 from the outside into the tower top of a water washing tower 5, performing water washing, and feeding purified oxidation liquid A2 flowing out from the tower top of the water washing tower out of the outside. Circulating alkali liquor B5 flowing out of the tower kettle of the alkaline washing tower is pressurized by a circulating alkali liquor pump 2 and returns to the top of the alkaline washing tower 1, discharging liquid B6 flowing out of the tower kettle of the alkaline washing tower enters an oil-water delayer 14 by pressurization of an alkaline washing tower kettle pump 3, oil-water demixing is carried out, an oil phase A5 flowing out of the delayer is merged with a mixed oxidizing liquid A1 and enters the tower kettle of the alkaline washing tower 1, and an aqueous phase flowing out of the delayer is sent out of the office as waste alkali liquor B2. The effluent C4 from the bottom of the water washing tower enters an oil-water separator 17 through the pressurization of a water washing tower bottom pump 6, the oil phase A9 of the effluent separator and the effluent A8 from the top of the alkaline washing tower are combined and enter the bottom of a water washing tower 5 through oil-water separation, and the water phase of the effluent separator is taken as wastewater C2 and is sent out. The material process parameters of the impure oxidation liquid before treatment and the purified oxidation liquid after treatment are shown in the table 1; the process equipment parameters of the caustic wash tower and the water wash tower are shown in Table 2.
Comparative example 2
Taking a commercial CHPPO industrial production device with nominal capacity of 10 ten thousand tons/year as an example, the prior art adopts a process flow of an alkaline washing tower and a water washing tower to treat the mixed oxidizing solution, and the process parameters of the mixed oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in Table 1; the process equipment parameters of the caustic wash tower and the water wash tower are shown in Table 2.
Comparative example 3
Taking a commercial CHPPO industrial production device with nominal capacity of 20 ten thousand tons/year as an example, the prior art adopts a process flow of an alkaline washing tower and a water washing tower to treat the mixed oxidizing solution, and the process parameters of the mixed oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in Table 1; the process equipment parameters of the caustic wash tower and the water wash tower are shown in Table 2.
Comparative example 4
Taking a commercial CHPPO industrial production device with nominal capacity of 40 ten thousand tons/year as an example, the prior art adopts a process flow of an alkaline washing tower and a water washing tower to treat the mixed oxidizing solution, and the process parameters of the mixed oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in Table 1; the process equipment parameters of the caustic wash tower and the water wash tower are shown in Table 2.
Comparative example 5
Taking a commercial CHPPO industrial production device with nominal capacity of 80 ten thousand tons/year as an example, the prior art adopts a process flow of an alkaline washing tower and a water washing tower to treat the mixed oxidizing solution, and the process parameters of the mixed oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in Table 1; the process equipment parameters of the caustic wash tower and the water wash tower are shown in Table 2.
Comparative example 6
Taking a commercial CHPPO industrial production device with nominal capacity of 40 ten thousand tons/year as an example, the prior art adopts a process flow of an alkaline washing tower and a water washing tower to treat the mixed oxidizing solution, and the process parameters of the mixed oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in Table 1; the process equipment parameters of the caustic wash tower and the water wash tower are shown in Table 2.
Comparative example 7
Taking a commercial CHPPO industrial production device with nominal capacity of 40 ten thousand tons/year as an example, the prior art adopts a process flow of an alkaline washing tower and a water washing tower to treat the mixed oxidizing solution, and the process parameters of the mixed oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in Table 1; the process equipment parameters of the caustic wash tower and the water wash tower are shown in Table 2.
[ example 1 ]
As shown in fig. 1, the present embodiment relates to a method for removing acid and sodium from a CHPPO device, which comprises the following steps: the impurity-containing oxidation liquid A1 of cumene hydroperoxide containing organic acid impurities and sodium ion impurities from the outside is combined with a pressurized water phase B4 of a delayer and enters a first mixer 11, a fresh lye B1 from the outside also enters the first mixer 11, a mixed discharge A3 of the first mixer enters a first centrifuge 13, the first centrifuge oil phase A4 which flows out after centrifugal separation enters an oil-water delayer 14 and is subjected to oil-water delamination, an effluent oil phase A5 of the delayer enters a second mixer 15, a fresh water C1 from the outside also enters the second mixer 15, a mixed discharge A6 of the second mixer enters a second centrifuge 16 and is subjected to centrifugal separation, an effluent oil phase A7 of the second centrifuge enters an oil-water separator 17, the oil-water separation is carried out, and an effluent oil phase is taken as a purified oxidation liquid A2 of the cumene hydroperoxide containing no organic acid impurities and sodium ion impurities and is sent out of the outside. The water phase B3 of the first centrifuge flowing out of the first centrifuge enters an oil-water demixer 14 for oil-water demixing, and the water phase B4 of the flowing-out demixer is pressurized by a demixer water phase pump 12 and then is combined with the mixed oxidation liquid A1 from the outside to enter a first mixer 11; the effluent waste lye B2 is discharged outside. The second centrifuge aqueous phase C3 flowing out of the second centrifuge enters the oil-water separator 17, is subjected to oil-water separation, and the outflow separator aqueous phase is sent out as wastewater C2.
The CHPPO device is a commercial industrial production device with nominal capacity of 5 ten thousand tons/year, and the material process parameters of the mixed oxidation liquid before treatment and the purified oxidation liquid after treatment are shown in a table 1; the process operating parameters are shown in Table 3; the process equipment parameters are shown in Table 4; the technical purposes of the embodiment are achieved by adopting the technical scheme of the alkaline washing process flow of the first mixer, the first centrifuge and the oil-water separator and the water washing process flow of the second mixer, the second centrifuge and the oil-water separator, the impurity content of organic acid of the purified oxidation liquid A2 is less than or equal to 50mg/kg, the impurity content of sodium ions is less than or equal to 1.0mg/kg, the investment of equipment engineering is saved by 66.64%, the operation cost is saved by 7.74%, and better technical effects are achieved.
[ example 2 ]
Similarly [ example 1 ], only the nominal capacity of the CHPPO apparatus was changed to 10 ten thousand tons/year in the commercial industrial production apparatus, and the process parameters of the materials of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in table 1; the process operating parameters are shown in Table 3; the process equipment parameters are shown in Table 4; the technical purposes of the embodiment are achieved by adopting the technical scheme of the alkaline washing process flow of the first mixer, the first centrifuge and the oil-water separator and the water washing process flow of the second mixer, the second centrifuge and the oil-water separator, the impurity content of organic acid of the purified oxidation liquid A2 is less than or equal to 50mg/kg, the impurity content of sodium ions is less than or equal to 1.0mg/kg, the investment of equipment engineering is saved by 66.88%, the operation cost is saved by 8.63%, and better technical effects are achieved.
[ example 3 ]
Similarly [ example 1 ], only the nominal capacity of the CHPPO apparatus was changed to 20 ten thousand tons/year in the commercial industrial production apparatus, and the process parameters of the materials of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in table 1; the process operating parameters are shown in Table 3; the process equipment parameters are shown in Table 4; by adopting the technical scheme of the alkaline washing process flow of the first mixer, the first centrifuge and the oil-water delaminator and the water washing process flow of the second mixer, the second centrifuge and the oil-water separator, the technical purposes of the embodiments are achieved, the impurity content of organic acid of the purified oxidation liquid A2 is less than or equal to 50mg/kg, the impurity content of sodium ions is less than or equal to 1.0mg/kg, the investment of equipment engineering is saved by 67.11%, the operation cost is saved by 10.49%, and better technical effects are achieved.
[ example 4 ]
Similarly [ example 1 ], only the nominal capacity of the CHPPO apparatus was changed to a commercial industrial production apparatus of 40 ten thousand tons/year, and the process parameters of the materials of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in table 1; the process operating parameters are shown in Table 3; the process equipment parameters are shown in Table 4; the technical purposes of the embodiment are achieved by adopting the technical scheme of the alkaline washing process flow of the first mixer, the first centrifuge and the oil-water delayer and the water washing process flow of the second mixer, the second centrifuge and the oil-water separator, the impurity content of organic acid of the purified oxidation liquid A2 is less than or equal to 50mg/kg, the impurity content of sodium ions is less than or equal to 1.0mg/kg, the investment of equipment engineering is saved by 67.42%, the operation cost is saved by 11.11%, and better technical effects are achieved.
[ example 5 ]
Similarly [ example 1 ], only the nominal capacity of the CHPPO apparatus was changed to 80 ten thousand tons/year in the commercial industrial production apparatus, and the process parameters of the materials of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in table 1; the process operating parameters are shown in Table 3; the process equipment parameters are shown in Table 4; by adopting the technical scheme of the alkaline washing process flow of the first mixer, the first centrifuge and the oil-water delaminator and the water washing process flow of the second mixer, the second centrifuge and the oil-water separator, the technical purposes of the embodiments are achieved, the impurity content of organic acid of the purified oxidation liquid A2 is less than or equal to 50mg/kg, the impurity content of sodium ions is less than or equal to 1.0mg/kg, the investment of equipment engineering is saved by 68.04%, the operation cost is saved by 11.73%, and better technical effects are achieved.
[ example 6 ]
Similarly [ example 4 ], the nominal capacity of the CHPPO plant is still 40 ten thousand tons/year for a commercial industrial production plant, only the process equipment parameters are changed, and the process parameters of the materials of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in table 1; the process operating parameters are shown in Table 3; the process equipment parameters are shown in Table 4; the technical purposes of the embodiment are achieved by adopting the technical scheme of the alkaline washing process flow of the first mixer, the first centrifuge and the oil-water separator and the water washing process flow of the second mixer, the second centrifuge and the oil-water separator, the impurity content of organic acid of the purified oxidation liquid A2 is less than or equal to 50mg/kg, the impurity content of sodium ions is less than or equal to 1.0mg/kg, the investment of equipment engineering is saved by 68.62%, the operation cost is saved by 10.41%, and better technical effects are achieved.
[ example 7 ]
Similarly [ example 4 ], the nominal capacity of the CHPPO plant is still 40 ten thousand tons/year for a commercial industrial production plant, only the process equipment parameters are changed, and the process parameters of the materials of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in table 1; the process operating parameters are shown in Table 3; the process equipment parameters are shown in Table 4; the technical purposes of the embodiment are achieved by adopting the technical scheme of the alkaline washing process flow of the first mixer, the first centrifuge and the oil-water separator and the water washing process flow of the second mixer, the second centrifuge and the oil-water separator, the impurity content of organic acid of the purified oxidation liquid A2 is less than or equal to 50mg/kg, the impurity content of sodium ions is less than or equal to 1.0mg/kg, the investment of equipment engineering is saved by 65.89%, the operation cost is saved by 10.85%, and better technical effects are achieved.
TABLE 1 summary of the parameters of the prior art and the materials before and after the treatment with the oxidizing solution of the present invention
TABLE 2 summary of process equipment parameters for alkaline and water wash towers of the prior art
TABLE 3 summary of operating parameters of the process equipment of the invention
TABLE 4 oil-water separator equipment parameter summary table of centrifuge oil-water delaminator of the invention
The embodiments of the present invention have been described in detail, but the embodiments are merely examples, and the present invention is not limited to the embodiments described above. It will be appreciated by those skilled in the art that any equivalent modifications and substitutions are within the scope of the present invention. Accordingly, equivalent changes and modifications made without departing from the spirit and scope of the present invention should be covered by the present invention.
Claims (9)
1. A method for separating acid and removing sodium from a CHPPO device is characterized in that the method comprises the following process flows in a large-scale commercial CHPPO industrial production device with nominal capacity of 5-80 ten thousand tons per year:
the heterogeneous oxidation liquid (A1) containing cumene hydroperoxide containing organic acid impurities and sodium ion impurities from the outside and the pressurized water phase (B4) of the delayer are combined and enter a first mixer (11), the fresh lye (B1) from the outside also enters a first mixer (11), the mixed discharge (A3) of the first mixer enters a first centrifuge (13), the first centrifuge oil phase (A4) which flows out after centrifugal separation enters an oil-water delayer (14), oil-water delaminating is carried out, the oil phase (A5) which flows out enters a second mixer (15), the fresh water (C1) from the outside also enters a second mixer (15), the discharge (A6) of the second mixer which is mixed enters a second centrifuge (16), the oil phase (A7) which flows out after centrifugal separation enters an oil-water separator (17), oil-water separation is carried out, and the oil phase which flows out as the purified liquid (A2) containing cumene hydroperoxide containing no organic acid impurities and sodium ion impurities ) Sending out the product outside the room;
the water phase (B3) of the first centrifuge flows out of the first centrifuge and enters an oil-water demixer (14) to be subjected to oil-water demixing, and the water phase (B4) of the outflow demixer is pressurized by a demixer water phase pump (12) and then is combined with the foreign oxidation-containing liquid (A1) from the outside to enter a first mixer (11); the effluent waste lye (B2) is sent out;
the second centrifuge water phase (C3) flowing out of the second centrifuge enters an oil-water separator (17) for oil-water separation, and the effluent separator water phase is sent out as waste water (C2).
2. The method for separating and removing acid and sodium from a CHPPO device as claimed in claim 1, wherein:
a) the mixed oxidation liquid (A1) containing organic acid impurities and sodium ion impurities from the outside and fresh alkali liquor (B1) flow and are divided, liquid drops are dispersed, liquid-liquid contact is carried out, radial mixing, blending diffusion and oil-water combination are carried out in a first mixer (11), and the organic acid impurities in the mixed oxidation liquid and the fresh alkali liquor (B1) are subjected to neutralization reaction and removed;
b) gathering and separating oil phase and water phase with different density by using centrifugal force generated by the rotation process of the first centrifuge (13), wherein the first centrifuge oil phase (A4) flowing out of the inner edge of the first centrifuge is allowed to contain a small amount of water phase, and the first centrifuge water phase (B3) flowing out of the outer edge of the first centrifuge is not allowed to contain oil phase;
c) the first centrifuge oil phase (A4) and the first centrifuge water phase (B3) respectively enter different parts of an oil-water separator, and the separator oil phase (A5) without water phase flows out of the top of the oil-water separator;
d) the demixer oil phase (A5) containing sodium ion impurities and the fresh water (C1) are subjected to flow division, droplet dispersion, liquid-liquid contact, radial mixing, blending diffusion and oil-water combination in the second mixer (15), and the sodium ion impurities in the demixer oil phase are dissolved and removed by the fresh water (C1);
e) gathering and separating the oil phase and the water phase with different densities by using the centrifugal force generated by the rotation process of the second centrifuge, wherein the oil phase (A7) of the second centrifuge flowing out from the inner edge of the second centrifuge is allowed to contain a small amount of the water phase, and the water phase (C3) of the second centrifuge flowing out from the outer edge of the second centrifuge is not allowed to contain the oil phase;
f) the second centrifuge oil phase (A7) and the second centrifuge water phase (C3) respectively enter different parts of the oil-water separator, and the demixer oil phase which flows out of the top of the oil-water separator and does not contain a water phase is taken as the purified oxidation liquid (A2) to be sent out.
3. The CHPPO device acid-removing and sodium-removing method as claimed in claim 1, wherein the cumene content of the mixed oxidation solution (A1) is 51.7-77.3 wt%, the cumene hydroperoxide CHP content is 20.0-38.0 wt%, the alpha, alpha-dimethyl benzyl alcohol DMBA content is 2.0-9.0 wt%, the light component content is 0.4-0.7 wt%, the heavy component content is 0.3-0.6 wt%, the organic acid content is 200-1000mg/kg, and the sodium ion content is 40-160 mg/kg.
4. The CHPPO device acid and sodium removal separation method as claimed in claim 1, wherein the first mixer (11) is operated at a pressure of 0.45-1.05MPaA and at a temperature of 25-85 ℃; the first centrifuge (13) is operated at a pressure of 0.40-1.00MPaA and at a temperature of 25-85 ℃; the operation pressure of the inlet of the water phase pump (12) of the delayer is 0.40-1.00MPaA, the operation pressure of the outlet is 0.55-1.15MPaA, and the operation temperature is 25-85 ℃; the operating pressure of the oil-water separator (14) is 0.38-0.98MPaA, and the operating temperature is 25-85 ℃.
5. The CHPPO device acid and sodium removal method as claimed in claim 4, wherein the first mixer (11) is operated at 0.55-0.95MPaA and 35-75 deg.C; the first centrifuge (13) is operated at a pressure of 0.50-0.90MPaA and at a temperature of 35-75 ℃; the operation pressure of the inlet of the water phase pump (12) of the delayer is 0.50-0.90MPaA, the operation pressure of the outlet is 0.65-1.05MPaA, and the operation temperature is 35-75 ℃; the operating pressure of the oil-water separator (14) is 0.48-0.88MPaA, and the operating temperature is 35-75 ℃.
6. The CHPPO device acid and sodium removal method as claimed in claim 5, wherein the first mixer (11) is operated at 0.65-0.85MPaA pressure and 45-65 deg.C; the first centrifuge (13) is operated at a pressure of 0.60-0.80MPaA and at a temperature of 45-65 ℃; the operation pressure of the inlet of the water phase pump (12) of the delayer is 0.60-0.80MPaA, the operation pressure of the outlet is 0.75-0.95MPaA, and the operation temperature is 45-65 ℃; the operating pressure of the oil-water separator (14) is 0.58-0.78MPaA, and the operating temperature is 45-65 ℃.
7. The CHPPO plant acid and sodium removal process as claimed in claim 1, wherein the second mixer (15) is operated at a pressure of 0.35-0.95MPaA and at a temperature of 25-85 ℃; the second centrifuge (16) operating at a pressure of 0.30-0.90MPaA and at a temperature of 25-85 ℃; the operating pressure of the oil-water separator (17) is 0.28-0.88MPaA, and the operating temperature is 25-85 ℃.
8. The CHPPO plant acid and sodium removal method as claimed in claim 7, wherein the second mixer (15) is operated at a pressure of 0.45-0.85MPaA and at a temperature of 35-75 ℃; the second centrifuge (16) is operated at a pressure of 0.40-0.80MPaA and at a temperature of 35-75 ℃; the operating pressure of the oil-water separator (17) is 0.38-0.78MPaA, and the operating temperature is 35-75 ℃.
9. The CHPPO plant acid and sodium removal process as claimed in claim 8, wherein the second mixer (15) is operated at a pressure of 0.55-0.75MPaA and at a temperature of 45-65 ℃; the second centrifuge (16) is operated at a pressure of 0.50-0.70MPaA and at a temperature of 45-65 ℃; the operating pressure of the oil-water separator (17) is 0.48-0.68MPaA, and the operating temperature is 45-65 ℃.
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Application publication date: 20201106 |