CN111763166A - System and method for deacidifying and removing sodium of CHPPO device - Google Patents
System and method for deacidifying and removing sodium of CHPPO device Download PDFInfo
- Publication number
- CN111763166A CN111763166A CN202010676357.7A CN202010676357A CN111763166A CN 111763166 A CN111763166 A CN 111763166A CN 202010676357 A CN202010676357 A CN 202010676357A CN 111763166 A CN111763166 A CN 111763166A
- Authority
- CN
- China
- Prior art keywords
- water
- oil
- hydrocyclone
- mixer
- liquid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims abstract description 103
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 title claims abstract description 28
- 239000011734 sodium Substances 0.000 title claims abstract description 28
- 229910052708 sodium Inorganic materials 0.000 title claims abstract description 28
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 158
- 239000007788 liquid Substances 0.000 claims abstract description 86
- 239000012071 phase Substances 0.000 claims abstract description 85
- 230000008569 process Effects 0.000 claims abstract description 62
- 230000003647 oxidation Effects 0.000 claims abstract description 34
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 34
- 229910001415 sodium ion Inorganic materials 0.000 claims abstract description 17
- 239000000463 material Substances 0.000 claims abstract description 16
- 150000007524 organic acids Chemical class 0.000 claims abstract description 14
- 239000008346 aqueous phase Substances 0.000 claims abstract description 9
- 238000000926 separation method Methods 0.000 claims description 47
- 239000012535 impurity Substances 0.000 claims description 38
- 239000003513 alkali Substances 0.000 claims description 29
- 238000002156 mixing Methods 0.000 claims description 21
- 239000013505 freshwater Substances 0.000 claims description 18
- 238000009776 industrial production Methods 0.000 claims description 18
- 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 17
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical compound [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 claims description 16
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 claims description 14
- 239000002699 waste material Substances 0.000 claims description 13
- 239000002351 wastewater Substances 0.000 claims description 11
- 238000007599 discharging Methods 0.000 claims description 9
- ARSRBNBHOADGJU-UHFFFAOYSA-N 7,12-dimethyltetraphene Chemical compound C1=CC2=CC=CC=C2C2=C1C(C)=C(C=CC=C1)C1=C2C ARSRBNBHOADGJU-UHFFFAOYSA-N 0.000 claims description 4
- VFZRZRDOXPRTSC-UHFFFAOYSA-N DMBA Natural products COC1=CC(OC)=CC(C=O)=C1 VFZRZRDOXPRTSC-UHFFFAOYSA-N 0.000 claims description 4
- 239000006185 dispersion Substances 0.000 claims description 3
- 238000006386 neutralization reaction 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
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- 238000005406 washing Methods 0.000 description 85
- 239000003921 oil Substances 0.000 description 52
- 230000001590 oxidative effect Effects 0.000 description 45
- 239000000243 solution Substances 0.000 description 33
- 239000007789 gas Substances 0.000 description 13
- 230000000694 effects Effects 0.000 description 11
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 description 10
- 239000003054 catalyst Substances 0.000 description 9
- 230000000052 comparative effect Effects 0.000 description 7
- 238000010521 absorption reaction Methods 0.000 description 6
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 5
- 239000005977 Ethylene Substances 0.000 description 5
- 238000004062 sedimentation Methods 0.000 description 5
- 238000004821 distillation Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000006735 epoxidation reaction Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 4
- 239000011541 reaction mixture Substances 0.000 description 4
- KWOLFJPFCHCOCG-UHFFFAOYSA-N Acetophenone Chemical compound CC(=O)C1=CC=CC=C1 KWOLFJPFCHCOCG-UHFFFAOYSA-N 0.000 description 3
- WVDDGKGOMKODPV-UHFFFAOYSA-N Benzyl alcohol Chemical compound OCC1=CC=CC=C1 WVDDGKGOMKODPV-UHFFFAOYSA-N 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- DNIAPMSPPWPWGF-UHFFFAOYSA-N Propylene glycol Chemical compound CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 description 3
- 239000003518 caustics Substances 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 3
- 238000004064 recycling Methods 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
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- 229920002472 Starch Polymers 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 235000019698 starch Nutrition 0.000 description 2
- 239000008107 starch Substances 0.000 description 2
- 239000011550 stock solution Substances 0.000 description 2
- 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
- NFPBWZOKGZKYRE-UHFFFAOYSA-N 2-propan-2-ylperoxypropane Chemical compound CC(C)OOC(C)C NFPBWZOKGZKYRE-UHFFFAOYSA-N 0.000 description 1
- OIGWAXDAPKFNCQ-UHFFFAOYSA-N 4-isopropylbenzyl alcohol Chemical compound CC(C)C1=CC=C(CO)C=C1 OIGWAXDAPKFNCQ-UHFFFAOYSA-N 0.000 description 1
- 239000004721 Polyphenylene oxide Substances 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 235000019445 benzyl alcohol Nutrition 0.000 description 1
- QGGZBXOADPVUPN-UHFFFAOYSA-N beta-phenylpropiophenone Natural products C=1C=CC=CC=1C(=O)CCC1=CC=CC=C1 QGGZBXOADPVUPN-UHFFFAOYSA-N 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 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
- 238000003912 environmental pollution Methods 0.000 description 1
- RTZKZFJDLAIYFH-UHFFFAOYSA-N ether Substances CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000003063 flame retardant Substances 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000007327 hydrogenolysis reaction Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 239000002245 particle 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
- 229920002635 polyurethane Polymers 0.000 description 1
- RUOJZAUFBMNUDX-UHFFFAOYSA-N propylene carbonate Chemical compound CC1COC(=O)O1 RUOJZAUFBMNUDX-UHFFFAOYSA-N 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
- 239000010689 synthetic lubricating oil Substances 0.000 description 1
- 229920006305 unsaturated polyester Polymers 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D301/00—Preparation of oxiranes
- C07D301/02—Synthesis of the oxirane ring
- C07D301/03—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds
- C07D301/19—Synthesis of the oxirane ring by oxidation of unsaturated compounds, or of mixtures of unsaturated and saturated compounds with organic hydroperoxides
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D303/00—Compounds containing three-membered rings having one oxygen atom as the only ring hetero atom
- C07D303/02—Compounds containing oxirane rings
- C07D303/04—Compounds containing oxirane rings containing only hydrogen and carbon atoms in addition to the ring oxygen atoms
Abstract
The invention relates to a system and a method for deacidifying and removing sodium in a CHPPO device, which mainly solve the problems of undefined process, incomplete flow, large equipment investment and high operating cost in the prior art. By adopting the system and the method, a mixer, a hydrocyclone, an oil-water layering/separator and a hydrocyclone knockout non-aqueous phase are arranged in a CHPPO device of 5-80 ten thousand tons per year, a small amount of oil phase is contained in the discharge material at the bottom of the hydrocyclone, purified oxidation liquid with organic acid of less than or equal to 50mg/kg and sodium ions of less than or equal to 1.0mg/kg is obtained after deacidification and sodium removal treatment, the equipment investment is saved by 40.00-44.43%, the operation cost is saved by 34.80-44.11%, the problems are well solved, and the system and the method can be applied to PO production in CHPPO industrial devices.
Description
Technical Field
The invention relates to the technical field of propylene oxide, in particular to a system and 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 cyclone 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 method for producing the isopropylbenzene by the invention with the patent application number of CN201310237099.2 in the prior art mainly solves the problems of poor stability of a catalyst and serious environmental pollution in the processes of benzyl alcohol hydrogenolysis and acetophenone hydrogenation in the prior art, adopts a hydrocarbon material containing α -dimethyl benzyl alcohol and acetophenone and hydrogen as raw materials, and has the advantages that the molar ratio of α -dimethyl benzyl alcohol in the hydrogen/hydrocarbon material is 5-15: 1, the reaction temperature is 150-250 ℃, the reaction pressure is 1.0-5.0 MPa, and the volume space velocity of the hydrocarbon material is 2.0-12.0 hours-1Under the condition that the raw material is sequentially mixed with catalyst A and catalystThe catalyst B is contacted with the catalyst B to react, wherein the catalyst A is a Pd/C catalyst, and the catalyst B is a Cu-based catalyst, so that the technical scheme better solves the problem, and can be used for industrial production of preparing the propylene oxide by an isopropyl peroxide method. The invention patent application No. CN201780046029.5 discloses a process for producing propylene oxide, which comprises (1) an oxidation step, (2) a distillation step, (3) an epoxidation step, and (4) a separation step, wherein the distillation step is a step of separating a reaction mixture containing cumene hydroperoxide obtained in the oxidation step into a distillate and a concentrated solution containing cumene hydroperoxide by distillation, and is a step of continuously distilling the reaction mixture under the condition that the ratio (D/F) of the flow rate (D) of the distillate to the flow rate (F) of the reaction mixture to be distilled is 0.037 or more and 0.13 or less, and the epoxidation step is a step of obtaining a reaction mixture containing propylene oxide and cumyl alcohol by contacting the concentrated solution containing cumene hydroperoxide obtained in the distillation step with propylene in 1 or more reactors in the presence of a catalyst to react the propylene with the cumene hydroperoxide in the concentrated solution, the method is a step of setting the outlet temperature of the final reactor of the 1 or more reactors to 115 ℃ or higher and less than 140 ℃. The invention patent application number is CN201910355724.0 static mixer, discloses at least including: the hollow mixer main body is provided with a liquid inlet and a liquid outlet in the length direction, a plurality of mixing units are sequentially communicated and arranged in the mixer main body and are hollow prisms. The static mixer has low fluid energy consumption, is not easy to cause the blockage of a pipeline, is suitable for miniaturization and has low cost. The invention patent application No. CN201380013225.4 centrifugal separator discloses a method and apparatus for optimizing a centrifugal separator, particularly for a recycle gas cyclone separator in a high temperature gasifier. The degree of separation of the centrifugal separator will be considerably increased. This is achieved according to the method, via an inner member on the dip tube of the centrifugal separator, such that a local increase of the centrifugal force is carried out. The invention discloses a hydrocyclone separator with the patent application number of CN201821614002.X, and relates to a hydrocyclone separator body, wherein the bottom end of the separator body is provided with a bottomThe flow tube, the below of separator body is provided with the holding vessel, the cavity has been seted up to the inside of holding vessel, the bottom and the cavity of underflow pipe are linked together, the coupling is installed on the top of holding vessel, install filter equipment on the roof of cavity, filter equipment includes the roof, the boss, the bottom plate, the filter screen, the filter core, be equipped with row material valve on the lateral wall of holding vessel, one side of holding vessel is provided with the stock solution box, the holding vessel leads to pipe with the stock solution box and is connected, this hydrocyclone separator is when separating starch thick liquid, the thick liquid that is mingled with solid particle gets into in the holding vessel along the underflow pipe under the effect of centrifugal force, and flow in the holding vessel after filter equipment's filtration, then can reuse by filterable thick liquid, the waste of starch thick. The invention discloses a centrifugal sedimentation separator with the patent application number of CN201920293119.0, which comprises a rotary separation device, an inlet pipe connected with one side of the rotary separation device, a clarified fluid outlet pipe arranged at the top end of the rotary separation device and a sedimentation separation tank arranged at the bottom end of the rotary separation device, wherein the rotary separation device comprises the rotary separation tank, at least two conical cylinders arranged at intervals up and down in the rotary separation tank, a clarified fluid ascending pipe connected with the bottom end of the rotary separation tank and jet pipes connected with the two sides of the rotary separation tank, the conical cylinders extend in a tapered shape from top to bottom along the inner wall of the rotary separation tank, the top ends of the two jet pipes are correspondingly arranged at the two sides of the conical cylinder at the uppermost layer in the rotary separation tank, the bottom ends of the two jet pipes are connected with the top end of the sedimentation separation tank, one end of the inlet pipe extends into the rotary separation tank and forms a tapered conical nozzle, the sedimentation separation, the bottom end of the conical body is connected with a discharge pipe. The centrifugal sedimentation separator has a simple structure and a higher separation effect. The invention discloses an oil-water separator with the patent application number of CN201811040353.9, which is used for improving the separation and purification quality and improving the treatment capacity of equipment. The device is installed in a vertical separation tank body and comprises a support plate, a guide plate and a separation layer, wherein the separation layer and the support plate are in a vertical circular ring shape, the lower end of the separation layer is fixed on an inclined pull beam, the upper end of the separation layer is connected with the inner wall of the separation tank body through an inclined pull beam, the guide plate is a solid plate and covers the annular separation layer, the support plate is in a circular ring shape, and the periphery of the support plate is in clearance fit with the inner wall of the separationAnd (6) mixing. The vertical oil-water separator with the structure has the advantages that the effective separation layer is designed into a circular ring shape, and the contact area of oil-water separation is greatly increased in the same tank space, so that the oil-water separation efficiency and the production processing capacity of equipment are greatly improved, the problem of long-term troubles in the oil-water separation process in oil refining chemical production is solved, and the vertical oil-water separator makes contributions to the improvement of product quality, the reduction of cost and the improvement of production efficiency. The invention has patent application number CN201110445155.2 a method for recycling ethylene gas from tail gas and its water alkaline washing tower, disclose a method for recycling ethylene gas from tail gas, it is tail gas from buffer tank (1) enter the lower section from the gas inlet (14), enter the middle section through the bypass air pipe (8) after finishing the exchange absorption with water, enter the upper section through the bypass air pipe (9) after finishing the exchange absorption with 1-3% alkali lye in this section, exchange the absorption again with water, send the gas holder (7) from the gas outlet (15) after purifying; water from the water circulation tank (3) firstly enters the upper section from a water inlet (16), enters the lower section through a bypass water pipe (10) after completing exchange absorption, and returns to the water circulation tank (3) from a water outlet (17) after completing exchange absorption; alkali liquor with the concentration of 1-3% from the alkali liquor circulating tank (5) enters the middle section from an alkali liquor inlet (18), and returns to the alkali liquor circulating tank (5) from an alkali liquor outlet (19) after exchange absorption is completed; the method can improve the content of the ethylene gas from 89.5 percent to 96.43 percent, and reduce the content of VAC from 9.49 percent to 2.57 percent.
The method for producing cumene through the invention patent application number CN201310237099.2 and the method for producing propylene oxide through the invention patent application number CN201780046029.5 in the prior art only disclose the production steps of cumene hydroperoxide, and do 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 has the technical scheme that a static mixer with the patent application number of CN201910355724.0, a centrifugal separator with the patent application number of CN201380013225.4, a hydrocyclone separator with the patent application number of CN201821614002, a centrifugal settling separator with the patent application number of CN201920293119.0 and an oil-water separator with the patent application number of CN201811040353.9 only disclose the operation function of a single device, and do not relate to a means for connecting the mixer, the hydrocyclone separator 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 a method for recovering ethylene gas from tail gas and a water caustic wash tower thereof with the patent application number of CN201110445155.2, and only discloses a method for treating the ethylene gas by adopting a caustic wash tower/water wash tower with large equipment engineering investment and high operation and running 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 system and a method for deacidifying and removing sodium in 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 system for deacidifying and removing sodium in a CHPPO device, which comprises the following components in a large-scale commercial CHPPO industrial production device with nominal capacity of 5-80 ten thousand tons per year:
the first mixer is used for dispersing the mixed oxidation liquid containing organic acid impurities and sodium ion impurities, the oil phase of the delayer and the fresh alkali liquor in a liquid drop manner, contacting the liquid with the liquid, combining the oil and the water, and fully mixing the liquid and the liquid, and the organic acid impurities in the oil phase of the mixed oxidation liquid and the delayer and the fresh alkali liquor are removed through neutralization reaction;
the first hydrocyclone is connected with the first mixer through a pipeline, the oil phase and the water phase with different densities are gathered and separated by using the centrifugal force generated in the hydrocyclone process, the top discharge of the first hydrocyclone does not allow the water-containing phase, and the bottom discharge of the first hydrocyclone allows a small amount of oil phase;
the first booster pump is connected with the first liquid cyclone through a pipeline and used for boosting the bottom discharge of the first liquid cyclone;
the oil-water demixer is connected with the first booster pump through a pipeline, the bottom discharge of the first hydrocyclone containing a small amount of oil phase is subjected to oil-water demixing, the oil phase of the demixer returns to the first mixer, and the water phase of the demixer is sent out as waste alkali liquor;
the second mixer is connected with the first hydrocyclone through a pipeline, the top discharge of the first hydrocyclone containing sodium ion impurities, the oil phase of the separator and the fresh water are subjected to liquid drop dispersion, liquid-liquid contact, oil-water combination and full mixing in the second mixer, and the sodium ion impurities in the top discharge of the first hydrocyclone and the oil phase of the separator are dissolved and removed by the fresh water;
the second hydrocyclone is connected with the second mixer through a pipeline, the oil phase and the water phase with different densities are gathered and separated by using the centrifugal force generated in the hydrocyclone process, the top discharge of the second hydrocyclone does not allow the water-containing phase, and the bottom discharge of the second hydrocyclone allows a small amount of oil phase; discharging from the top of the second cyclone as purified oxidizing liquid and discharging to the outside;
the second booster pump is connected with the second liquid cyclone through a pipeline and used for boosting the discharge at the bottom of the second liquid cyclone;
and the oil-water separator is connected with the second booster pump through a pipeline, the oil-water separation is carried out on the discharged material at the bottom of the second hydrocyclone containing a small amount of oil phase, the oil phase of the separator returns to the second mixer, and the water phase of the separator is taken as wastewater to be discharged outside.
The second aspect of the invention provides a deacidification and sodium removal method for a CHPPO device, which comprises the following process flows of:
a. mixing the mixed oxidation liquid from the outside with the oil of the demixer, and then mixing with the fresh lye from the outside to enter a first mixer; the mixed first mixer discharges into a first hydrocyclone, the top discharge of the first hydrocyclone after hydrocyclone separation is combined with fresh water from outside, and then is combined with the separator oil and enters a second mixer, the mixed second mixer discharges into a second hydrocyclone, and the purified oxidation liquid flowing out of the top of the second hydrocyclone after hydrocyclone separation is discharged outside;
b. the bottom discharge material of the first hydrocyclone flowing out from the bottom of the first hydrocyclone is pressurized by a first booster pump and then enters an oil-water demixer, is subjected to oil-water demixing, the oil phase of the outflowing demixer is combined with the mixed oxidation liquid, and is combined with fresh alkali liquor from outside and enters a first mixer; the effluent water phase of the delaminator is taken as waste lye and sent out of the room;
c. the bottom discharge material of the second hydrocyclone flowing out from the bottom of the second hydrocyclone is pressurized by a second booster pump and then enters an oil-water separator, and after oil-water separation, the oil phase of the outflow separator, the top discharge material of the first hydrocyclone and fresh water from outside are combined and enter a second mixer; the effluent separator water phase is sent out as waste water.
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 0.22-0.82MPaA and at a temperature of 25-85 ℃; the operating pressure of the first cyclone is 0.20-0.80MPaA, and the operating temperature is 25-85 ℃; the inlet operating pressure of the first booster pump is 0.20-0.80MPaA, the outlet operating pressure is 0.35-0.95MPaA, and the operating temperature is 25-85 ℃; the operating pressure of the oil-water delaminator is 0.30-0.90MPaA, and the operating temperature is 25-85 ℃.
Further preferably, the first mixer is operated at a pressure of 0.32-0.72MPaA and at a temperature of 35-75 ℃; the operating pressure of the first cyclone is 0.30-0.70MPaA, and the operating temperature is 35-75 ℃; the inlet operating pressure of the first booster pump is 0.30-0.70MPaA, the outlet operating pressure is 0.45-0.85MPaA, and the operating temperature is 35-75 ℃; the operating pressure of the oil-water separator is 0.40-0.80MPaA, and the operating temperature is 35-75 ℃.
More preferably, the first mixer is operated at a pressure of 0.42 to 0.62MPaA and at a temperature of 45 to 65 ℃; the operating pressure of the first cyclone is 0.40-0.60MPaA, and the operating temperature is 45-65 ℃; the inlet operating pressure of the first booster pump is 0.40-0.60MPaA, the outlet operating pressure is 0.55-0.75MPaA, and the operating temperature is 45-65 ℃; the operating pressure of the oil-water separator is 0.50-0.70MPaA, and the operating temperature is 45-65 ℃.
Further, the second mixer is operated at a pressure of 0.17-0.77MPaA and at a temperature of 25-85 ℃; the operating pressure of the second cyclone is 0.15-0.75MPaA, and the operating temperature is 25-85 ℃; the inlet operating pressure of the second booster pump is 0.15-0.75MPaA, the outlet operating pressure is 0.30-0.90MPaA, and the operating temperature is 25-85 ℃; the operating pressure of the oil-water separator is 0.25-0.85MPaA, and the operating temperature is 25-85 ℃.
Further preferably, the second mixer is operated at a pressure of 0.27 to 0.67MPaA and at a temperature of 35 to 75 ℃; the operating pressure of the second cyclone is 0.25-0.65MPaA, and the operating temperature is 35-75 ℃; the inlet operating pressure of the second booster pump is 0.25-0.65MPaA, the outlet operating pressure is 0.40-0.80MPaA, and the operating temperature is 35-75 ℃; the operating pressure of the oil-water separator is 0.35-0.75MPaA, and the operating temperature is 35-75 ℃.
More preferably, the second mixer is operated at a pressure of 0.37 to 0.57MPaA and at a temperature of 45 to 65 ℃; the operating pressure of the second cyclone is 0.35-0.55MPaA, and the operating temperature is 45-65 ℃; the inlet operating pressure of the second booster pump is 0.35-0.55MPaA, the outlet operating pressure is 0.50-0.70MPaA, and the operating temperature is 45-65 ℃; the operating pressure of the oil-water separator is 0.45-0.65MPaA, 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 system and a method for deacidifying and removing sodium of a CHPPO device, for a large-scale commercial CHPPO industrial production device with nominal capacity of 5-80 ten thousand tons/year, a 'first mixer-first hydrocyclone-oil-water demixer' alkaline washing process flow and a 'second mixer-second hydrocyclone-oil-water separator' water washing process flow are adopted to replace the 'alkaline washing tower-water washing tower' process flow in the prior art, the discharge at the top of the hydrocyclone is set not to allow an aqueous phase, the discharge at the bottom of the hydrocyclone is allowed to contain a small amount of oil phase, the cumene hydroperoxide impurity-containing liquid containing 200-containing organic acid impurities and 40-160mg/kg sodium ion impurities is deacidified and removed with sodium 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, the investment of equipment engineering can be saved by 40.00-44.43%, the operating cost can be saved by 34.80-44.11%, and better technical effect can be achieved.
Drawings
FIG. 1 is a schematic process flow diagram of the present invention;
wherein, 11-a first mixer, 12-a first hydrocyclone, 13-a first booster pump, 14-an oil-water delayer, 15-a second mixer, 16-a second hydrocyclone, 17-a second booster pump, 18-an oil-water separator, A1-a mixed oxidizing liquid, A2-a purified oxidizing liquid, A3-a discharge of the first mixer, A4-a top discharge of the first hydrocyclone, A5-a delayer oil phase, A6-a discharge of the second mixer, A7-a separator oil phase, B1-an alkali liquor fresh, B2-a waste alkali liquor, B3-a bottom discharge of the first hydrocyclone, C1-fresh water, C2-wastewater, C3-a bottom discharge of the second hydrocyclone;
the process flow of the invention is described as follows:
the mixed oxidation liquid A1 from the outside is combined with the oil phase A5 of the demixer, and then is combined with the fresh lye B1 from the outside to enter the first mixer 11, the mixed discharge A3 of the first mixer enters the first hydrocyclone 12, the top discharge A4 of the first hydrocyclone after hydrocyclone separation is combined with the fresh water C1 from the outside, and then is combined with the oil phase A7 of the separator to enter the second mixer 15, the mixed discharge A6 of the second mixer enters the second hydrocyclone 16, and the purified oxidation liquid A2 flowing out from the top of the second hydrocyclone after hydrocyclone separation is sent out of the outside. A first hydrocyclone bottom discharge B3 flowing out of the first hydrocyclone bottom is pressurized by a first booster pump 13 and then enters an oil-water demixer 14, oil-water demixing is carried out, an outflowing demixer oil phase A5 is combined with a mixed oxidation liquid A1, and then the mixed oxidation liquid and fresh alkali liquor B1 from the outside are combined and enter a first mixer 11; the effluent aqueous phase of the separator was taken out as waste B2. A second hydrocyclone bottom discharge C3 flowing out of the second hydrocyclone bottom is pressurized by a second booster pump 17 and then enters an oil-water separator 18, and after oil-water separation, an effluent separator oil phase A7, a first hydrocyclone top discharge A4 and fresh water C1 from outside are combined and enter a second mixer 15; the effluent separator aqueous phase was sent to the outside as waste water C2.
FIG. 2 is a schematic process flow diagram of the prior art;
the method comprises the following steps of 1-an alkaline washing tower, 2-a circulating lye pump, 3-an alkaline washing tower kettle pump, 14-an oil-water delayer, 5-a water washing tower, 6-a water washing tower kettle pump, 18-an oil-water separator, A1-a miscellaneous oxidizing liquid, A2-a purified oxidizing liquid, A8-an alkaline washing tower top discharge, A5-a delayer oil phase, A7-a separator oil phase, B1-a fresh alkali liquid, B2-a waste alkali liquid, B5-a circulating alkali liquid, B4-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 A7 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 B4 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 18 through the pressurization of a water washing tower bottom pump 6, the oil phase A7 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 system and a method for deacidifying and removing sodium of 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.
[ example 1 ]
As shown in fig. 1, the present embodiment provides a system for deacidifying and removing sodium in a CHPPO apparatus, which specifically includes the following technical contents:
(1) the first mixer 11, the impurity-containing oxidizing liquid A1 containing organic acid impurities and sodium ion impurities, the delayer oil phase A5 and the fresh lye B1 are dispersed in the first mixer 11, contacted with liquid and liquid, combined with oil and water and fully mixed, and the organic acid impurities in the impurity-containing oxidizing liquid A1 and the delayer oil phase A5 and the fresh lye B1 are removed by neutralization reaction;
(2) the first hydrocyclone 12 is connected with the first mixer 11 through a pipeline, the oil phase and the water phase with different densities are gathered and separated by using the centrifugal force generated in the hydrocyclone 12 in the hydrocyclone process, the top discharge A4 of the first hydrocyclone does not allow the water-containing phase, and the bottom discharge B3 of the first hydrocyclone allows the oil phase with a small content;
(3) the first booster pump 13 is connected with the first liquid cyclone 12 through a pipeline and boosts the bottom discharge B3 of the first liquid cyclone;
(4) the oil-water demixer 14 is connected with the first booster pump 13 through a pipeline, oil-water demixing is carried out on a first hydrocyclone bottom discharge B3 containing a small amount of oil phase, a demixer oil phase A5 returns to the first mixer 11, and a demixer water phase is sent out as waste alkali liquid B2;
(5) the second mixer 15 is connected with the first cyclone 12 through a pipeline, the first cyclone top discharge A4 containing sodium ion impurities, the separator oil phase A7 and the fresh water C1 are subjected to liquid drop dispersion, liquid-liquid contact, oil-water combination and full mixing in the second mixer 15, and the sodium ion impurities in the first cyclone top discharge A4 and the separator oil phase A7 are dissolved and removed by the fresh water C1;
(6) the second hydrocyclone 16 is connected with the second mixer 15 through a pipeline, the oil phase and the water phase with different densities are gathered and separated by using the centrifugal force generated in the hydrocyclone 16 in the hydrocyclone process, the top discharge A2 of the second hydrocyclone does not allow the water-containing phase, and the bottom discharge C3 of the second hydrocyclone allows the oil phase with a small amount; the top discharge of the second cyclone is taken as purified oxidation liquid A2 and is discharged to the outside;
(7) the second booster pump 17 is connected with the second hydrocyclone 16 through a pipeline and boosts the bottom discharge C3 of the second hydrocyclone;
(8) the oil-water separator 18 is connected with the second booster pump 17 through a pipeline, oil-water separation is carried out on the second hydrocyclone bottom discharge C3 containing a small amount of oil phase, the separator oil phase A7 returns to the second mixer 15, and the separator water phase is sent out as wastewater B2.
[ example 2 ]
As shown in fig. 1, the embodiment provides a method for deacidifying and removing sodium in a CHPPO device, which specifically includes the following process flows:
a. mixing the foreign oxidizing liquid A1 from the outside with the oil phase A5 of the demixer, then mixing with the fresh lye B1 from the outside, entering a first mixer 11, mixing the discharge A3 of the first mixer with a first cyclone 12, mixing the top discharge A4 of the first cyclone after cyclone separation with the fresh water C1 from the outside, then mixing with the oil phase A7 of the separator, entering a second mixer 15, mixing the discharge A6 of the second mixer with a second cyclone 16, and sending the purified oxidizing liquid A2 flowing out from the top of the second cyclone after cyclone separation out of the outside;
b. a first hydrocyclone bottom discharge B3 flowing out of the first hydrocyclone bottom is pressurized by a first booster pump 13 and then enters an oil-water demixer 14, oil-water demixing is carried out, an outflowing demixer oil phase A5 is combined with a mixed oxidation liquid A1, and then the mixed oxidation liquid and fresh alkali liquor B1 from the outside are combined and enter a first mixer 11; the effluent water phase of the demixer is taken as waste lye B2 and is sent out of the room;
c. a second hydrocyclone bottom discharge C3 flowing out of the second hydrocyclone bottom is pressurized by a second booster pump 17 and then enters an oil-water separator 18, and after oil-water separation, an effluent separator oil phase A7, a first hydrocyclone top discharge A4 and fresh water C1 from outside are combined and enter a second mixer 15; the effluent separator aqueous phase was sent to the outside as waste water C2.
[ example 3 ]
This example provides an application example based on the above-mentioned deacidification and sodium removal system and method for a CHPPO apparatus, which is a commercial industrial production apparatus with nominal capacity of 5 ten thousand tons/year, and the process equipment parameters, as shown in tables 3 and 4; the process parameters of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in Table 2; by adopting the technical scheme of the alkaline washing process flow of the first mixer, the first hydrocyclone and the oil-water delaminator and the water washing process flow of the second mixer, the second hydrocyclone and the oil-water separator, the technical purposes of the embodiments are achieved, the equipment engineering investment is saved by 41.12%, the operation cost is saved by 34.80%, and better technical effects are achieved.
[ example 4 ]
This example provides an application example based on the above-mentioned deacidification and sodium removal system and method for a CHPPO apparatus, which is a commercial industrial production apparatus with nominal capacity of 10 ten thousand tons/year, and the process equipment parameters, as shown in tables 3 and 4; the process parameters of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in Table 2; by adopting the technical scheme of the alkaline washing process flow of the first mixer, the first hydrocyclone and the oil-water delaminator and the water washing process flow of the second mixer, the second hydrocyclone and the oil-water separator, the technical purposes of the embodiments are achieved, the equipment engineering investment is saved by 41.62%, the operation cost is saved by 36.35%, and better technical effects are achieved.
[ example 5 ]
This example provides an application example based on the above-mentioned deacidification and sodium removal system and method for a CHPPO apparatus, which is a commercial industrial production apparatus with a nominal capacity of 20 ten thousand tons/year, and the process equipment parameters, as shown in tables 3 and 4; the process parameters of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in Table 2; by adopting the technical scheme of the alkaline washing process flow of the first mixer, the first hydrocyclone and the oil-water delaminator and the water washing process flow of the second mixer, the second hydrocyclone and the oil-water separator, the technical purposes of the embodiments are achieved, the equipment engineering investment is saved by 42.22%, the operation cost is saved by 39.46%, and better technical effects are achieved.
[ example 6 ]
This example provides an application example based on the above-mentioned deacidification and sodium removal system and method for a CHPPO apparatus, which is a commercial industrial production apparatus with a nominal capacity of 40 ten thousand tons/year, and the process equipment parameters, as shown in tables 3 and 4; the process parameters of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in Table 2; by adopting the technical scheme of the alkaline washing process flow of the first mixer, the first hydrocyclone and the oil-water delaminator and the water washing process flow of the second mixer, the second hydrocyclone and the oil-water separator, the technical purposes of the embodiments are achieved, the equipment engineering investment is saved by 43.05%, the operation and running cost is saved by 41.01%, and better technical effects are achieved.
[ example 7 ]
This example provides an application example based on the above-mentioned deacidification and sodium removal system and method for a CHPPO apparatus, which is a commercial industrial production apparatus with nominal capacity of 80 ten thousand tons/year, and the process equipment parameters, as shown in tables 3 and 4; the process parameters of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in Table 2; by adopting the technical scheme of the alkaline washing process flow of the first mixer, the first hydrocyclone and the oil-water delaminator and the water washing process flow of the second mixer, the second hydrocyclone and the oil-water separator, the technical purposes of the embodiments are achieved, the equipment engineering investment is saved by 43.95%, the operation cost is saved by 44.11%, and better technical effects are achieved.
[ example 8 ]
This example provides an application example based on the above-mentioned deacidification and sodium removal system and method for a CHPPO apparatus, which is a commercial industrial production apparatus with a nominal capacity of 40 ten thousand tons/year, and the process equipment parameters, as shown in tables 3 and 4; the process parameters of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in Table 2; by adopting the technical scheme of the alkaline washing process flow of the first mixer, the first hydrocyclone and the oil-water delaminator and the water washing process flow of the second mixer, the second hydrocyclone and the oil-water separator, the technical purposes of the embodiments are achieved, the equipment engineering investment is saved by 44.43%, the operation cost is saved by 38.63%, and better technical effects are achieved.
[ example 9 ]
This example provides an application example based on the above-mentioned deacidification and sodium removal system and method for a CHPPO apparatus, which is a commercial industrial production apparatus with a nominal capacity of 40 ten thousand tons/year, and the process equipment parameters, as shown in tables 3 and 4; the process parameters of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in Table 2; by adopting the technical scheme of the alkaline washing process flow of the first mixer, the first hydrocyclone and the oil-water delaminator and the water washing process flow of the second mixer, the second hydrocyclone and the oil-water separator, the technical purposes of the embodiments are achieved, the equipment engineering investment is saved by 40.00%, the operation and running cost is saved by 40.32%, and better technical effects are achieved.
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 the impurity-containing oxidation liquid A1 from the outside with the oil phase A5 of the demixer, feeding the mixture into the tower kettle of the alkaline washing tower 1, mixing the fresh alkaline liquor B1 from the outside with the circulating alkaline liquor B5, feeding the mixture into the tower top of the alkaline washing tower 1, carrying out alkaline washing, mixing the A8 flowing out from the tower top of the alkaline washing tower with the oil phase A7 of the separator, feeding the fresh water C1 from the outside into the tower top of the water washing tower 5, washing with water, and feeding the 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 B4 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 18 through the pressurization of a water washing tower bottom pump 6, the oil phase A7 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 parameters of the process equipment of the alkaline washing tower and the water washing tower are shown in the table 1; the process parameters of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment 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 oxidation liquid containing impurities, and the process equipment parameters of the alkaline washing tower and the water washing tower are shown in Table 1; the process parameters of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment 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 oxidation liquid containing impurities, and the process equipment parameters of the alkaline washing tower and the water washing tower are shown in Table 1; the process parameters of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment 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 oxidation liquid containing impurities, and the process equipment parameters of the alkaline washing tower and the water washing tower are shown in Table 1; the process parameters of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment 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-a water washing tower' to treat the oxidation liquid containing impurities, and the process equipment parameters of the alkaline washing tower and the water washing tower are shown in Table 1; the process parameters of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment 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 oxidation liquid containing impurities, and the process equipment parameters of the alkaline washing tower and the water washing tower are shown in Table 1; the process parameters of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment 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 oxidation liquid containing impurities, and the process equipment parameters of the alkaline washing tower and the water washing tower are shown in Table 1; the process parameters of the impure oxidizing solution before treatment and the purified oxidizing solution after treatment are shown in Table 2.
TABLE 1 summary of process equipment parameters for alkaline and water wash towers of the prior art
TABLE 2 summary of the Process parameters before and after treatment of the oxidizing solution of the present invention
Table 3 summary of process parameters of the mixer cyclone hydro-extractor of the present invention
Table 4 summary of the parameters of the cyclone oil-water separator/stratifying device of the present 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 system for deacidifying and removing sodium in a CHPPO device is characterized by comprising the following components in a large-scale commercial CHPPO industrial production device with nominal capacity of 5-80 ten thousand tons per year:
the first mixer is used for dispersing the mixed oxidation liquid containing organic acid impurities and sodium ion impurities, the oil phase of the delayer and the fresh alkali liquor in a liquid drop manner, contacting the liquid with the liquid, combining the oil and the water, and fully mixing the liquid and the liquid, and the organic acid impurities in the oil phase of the mixed oxidation liquid and the delayer and the fresh alkali liquor are removed through neutralization reaction;
the first hydrocyclone is connected with the first mixer through a pipeline, the oil phase and the water phase with different densities are gathered and separated by using the centrifugal force generated in the hydrocyclone process, the top discharge of the first hydrocyclone does not allow the water-containing phase, and the bottom discharge of the first hydrocyclone allows a small amount of the oil phase;
the first booster pump is connected with the first liquid cyclone through a pipeline and used for boosting the bottom discharge of the first liquid cyclone;
the oil-water demixer is connected with the first booster pump through a pipeline, discharges the first hydrocyclone bottom material containing a small amount of oil phase and carries out oil-water demixing, the oil phase of the demixer returns to the first mixer, and the water phase of the demixer is taken as waste alkali liquor and is discharged out of the room;
the second mixer is connected with the first cyclone through a pipeline, the top discharge of the first cyclone containing sodium ion impurities, the oil phase of the separator and fresh water are subjected to liquid drop dispersion, liquid-liquid contact, oil-water combination and full mixing in the second mixer, and the sodium ion impurities in the top discharge of the first cyclone and the oil phase of the separator are dissolved and removed by the fresh water;
the second hydrocyclone is connected with the second mixer through a pipeline, the oil phase and the water phase with different densities are gathered and separated by using the centrifugal force generated in the hydrocyclone process, the top discharge of the second hydrocyclone does not allow the water-containing phase, and the bottom discharge of the second hydrocyclone allows a small amount of the oil phase; the top discharge of the second cyclone is taken as purified oxidation liquid and is sent out of the room;
the second booster pump is connected with the second liquid cyclone through a pipeline and used for boosting the discharge at the bottom of the second liquid cyclone;
and the oil-water separator is connected with the second booster pump through a pipeline, the oil-water separation is carried out on the discharged material at the bottom of the second hydrocyclone containing a small amount of oil phase, the oil phase of the separator returns to the second mixer, and the water phase of the separator is taken as wastewater to be discharged outside.
2. A method for deacidifying and removing sodium by using a CHPPO device of the system of claim 1, which is characterized by comprising the following process flows:
a. the mixed oxidation liquid from the outside is combined with the oil of the demixer and then is combined with the fresh lye from the outside to enter the first mixer; discharging the mixed first mixer to enter a first hydrocyclone, combining the top discharging material of the first hydrocyclone after hydrocyclone separation with the fresh water from outside, combining the top discharging material of the first hydrocyclone with the oil of the separator, entering a second mixer, discharging the mixed second mixer to enter a second hydrocyclone, and discharging the purified oxidation liquid flowing out of the top of the second hydrocyclone after hydrocyclone separation to outside;
b. the bottom discharge material of the first hydrocyclone flowing out from the bottom of the first hydrocyclone is pressurized by the first booster pump and then enters the oil-water demixer, is subjected to oil-water demixing, and the oil phase of the flowing-out demixer is combined with the mixed oxidation liquid and then is combined with the fresh alkali liquor from outside and enters the first mixer; the effluent aqueous phase of the demixer is taken as waste alkali liquor and sent out of the room;
c. the bottom discharge material of the second hydrocyclone flowing out from the bottom of the second hydrocyclone is pressurized by the second booster pump and then enters the oil-water separator, and after oil-water separation, the oil phase of the outflow separator, the top discharge material of the first hydrocyclone and the fresh water from the outside are combined and enter the second mixer; the effluent aqueous phase of the separator is discharged to the outside as waste water.
3. The method for deacidifying and removing sodium in a CHPPO device as claimed in claim 2, wherein the cumene content of the solution containing the impurity 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 method for deacidifying and removing sodium from a CHPPO device as claimed in claim 2, wherein said first mixer is operated at a pressure of 0.22-0.82MPaA and an operating temperature of 25-85 ℃; the operating pressure of the first cyclone is 0.20-0.80MPaA, and the operating temperature is 25-85 ℃; the inlet operating pressure of the first booster pump is 0.20-0.80MPaA, the outlet operating pressure is 0.35-0.95MPaA, and the operating temperature is 25-85 ℃; the operating pressure of the oil-water delaminator is 0.30-0.90MPaA, and the operating temperature is 25-85 ℃.
5. The method for deacidifying and removing sodium from a CHPPO device according to claim 4, wherein the first mixer is operated at a pressure of 0.32-0.72MPaA and at a temperature of 35-75 ℃; the operating pressure of the first cyclone is 0.30-0.70MPaA, and the operating temperature is 35-75 ℃; the inlet operating pressure of the first booster pump is 0.30-0.70MPaA, the outlet operating pressure is 0.45-0.85MPaA, and the operating temperature is 35-75 ℃; the operating pressure of the oil-water delaminator is 0.40-0.80MPaA, and the operating temperature is 35-75 ℃.
6. The method for deacidifying and removing sodium from a CHPPO device according to claim 5, wherein the first mixer is operated at a pressure of 0.42-0.62MPaA and at a temperature of 45-65 ℃; the operating pressure of the first cyclone is 0.40-0.60MPaA, and the operating temperature is 45-65 ℃; the inlet operating pressure of the first booster pump is 0.40-0.60MPaA, the outlet operating pressure is 0.55-0.75MPaA, and the operating temperature is 45-65 ℃; the operating pressure of the oil-water delaminator is 0.50-0.70MPaA, and the operating temperature is 45-65 ℃.
7. The method for deacidifying and removing sodium from a CHPPO device according to claim 2, wherein the second mixer is operated at a pressure of 0.17-0.77MPaA and at a temperature of 25-85 ℃; the operating pressure of the second cyclone is 0.15-0.75MPaA, and the operating temperature is 25-85 ℃; the inlet operating pressure of the second booster pump is 0.15-0.75MPaA, the outlet operating pressure is 0.30-0.90MPaA, and the operating temperature is 25-85 ℃; the operating pressure of the oil-water separator is 0.25-0.85MPaA, and the operating temperature is 25-85 ℃.
8. The method for deacidifying and removing sodium from a CHPPO device according to claim 7, wherein the second mixer is operated at a pressure of 0.27-0.67MPaA and at a temperature of 35-75 ℃; the operating pressure of the second cyclone is 0.25-0.65MPaA, and the operating temperature is 35-75 ℃; the inlet operating pressure of the second booster pump is 0.25-0.65MPaA, the outlet operating pressure is 0.40-0.80MPaA, and the operating temperature is 35-75 ℃; the oil-water separator has the operation pressure of 0.35-0.75MPaA and the operation temperature of 35-75 ℃.
9. The method for deacidifying and removing sodium from a CHPPO device according to claim 8, wherein the second mixer is operated at a pressure of 0.37-0.57MPaA and at a temperature of 45-65 ℃; the operating pressure of the second cyclone is 0.35-0.55MPaA, and the operating temperature is 45-65 ℃; the inlet operating pressure of the second booster pump is 0.35-0.55MPaA, the outlet operating pressure is 0.50-0.70MPaA, and the operating temperature is 45-65 ℃; the operating pressure of the oil-water separator is 0.45-0.65MPaA, and the operating temperature is 45-65 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010676357.7A CN111763166A (en) | 2020-07-14 | 2020-07-14 | System and method for deacidifying and removing sodium of CHPPO device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010676357.7A CN111763166A (en) | 2020-07-14 | 2020-07-14 | System and method for deacidifying and removing sodium of CHPPO device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111763166A true CN111763166A (en) | 2020-10-13 |
Family
ID=72725419
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010676357.7A Pending CN111763166A (en) | 2020-07-14 | 2020-07-14 | System and method for deacidifying and removing sodium of CHPPO device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111763166A (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101108794A (en) * | 2007-08-16 | 2008-01-23 | 华东理工大学 | Method for prolonging cycle of oparation of pimelinketone device and equipment thereof |
| CN104109140A (en) * | 2013-04-16 | 2014-10-22 | 中国石油化工股份有限公司 | Epoxypropane production method |
| WO2016127274A1 (en) * | 2015-02-09 | 2016-08-18 | 华东理工大学 | Step-by-step oil-water mixture separation method coupled with oil gas washing |
| CN110627935A (en) * | 2018-06-25 | 2019-12-31 | 中国石化工程建设有限公司 | Purification device and purification method for poly alpha-olefin reaction product |
| CN111116341A (en) * | 2019-12-12 | 2020-05-08 | 上海灿越化工科技有限公司 | Method and device for deeply removing impurities in oxidizing liquid |
-
2020
- 2020-07-14 CN CN202010676357.7A patent/CN111763166A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101108794A (en) * | 2007-08-16 | 2008-01-23 | 华东理工大学 | Method for prolonging cycle of oparation of pimelinketone device and equipment thereof |
| CN104109140A (en) * | 2013-04-16 | 2014-10-22 | 中国石油化工股份有限公司 | Epoxypropane production method |
| WO2016127274A1 (en) * | 2015-02-09 | 2016-08-18 | 华东理工大学 | Step-by-step oil-water mixture separation method coupled with oil gas washing |
| CN110627935A (en) * | 2018-06-25 | 2019-12-31 | 中国石化工程建设有限公司 | Purification device and purification method for poly alpha-olefin reaction product |
| CN111116341A (en) * | 2019-12-12 | 2020-05-08 | 上海灿越化工科技有限公司 | Method and device for deeply removing impurities in oxidizing liquid |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111848325B (en) | Method and system for alkaline washing of cumene raw material by CHPPO device | |
| RU2756585C2 (en) | Purification of waste stream in technological process of joint production of propylene oxide and styrene | |
| CN113003847A (en) | Treatment method for wastewater generated in production of propylene oxide by co-oxidation method | |
| CN111763167B (en) | Method for separating trace impurities by CHPPO device | |
| CN111807920A (en) | Method and system for deacidifying cumene raw material of CHPPO (chlorinated Polypropylene oxide) device | |
| CN102408913B (en) | Light hydrocarbon sweetening process utilizing alkali liquor by stages | |
| CN111056903B (en) | Process and device for recovering benzene partial hydrogenation catalyst | |
| CN111763166A (en) | System and method for deacidifying and removing sodium of CHPPO device | |
| CN111892523A (en) | Method for removing acid and sodium by CHPPO device | |
| CN111732083A (en) | Fluidized bed hydrogen peroxide process | |
| CN111574342A (en) | Enhanced reaction system and method for preparing cyclohexanone by selective hydrogenation of benzene | |
| CN114100544B (en) | Organic hydrocarbon peroxide treatment device and treatment method | |
| CN111875529A (en) | System and method for removing trace waste by CHPPO device | |
| CN1227198C (en) | Method for preparing relevant alcohol and ketone by adding hydrogen into hydroperoxide of hydrocarbon | |
| CN212334901U (en) | Methanol synthesis alkene wastewater treatment recycling system | |
| CN111333216B (en) | Treatment and reuse process of methanol-to-olefin wastewater | |
| CN111874869A (en) | Preparation process for preparing hydrogen peroxide from novel working solution | |
| CN211813946U (en) | Processing system of industry alkali dreg waste water | |
| CN116462563A (en) | Raw material treatment method for producing CHP by peroxidation of isopropylbenzene | |
| CN113512013B (en) | System and method for preparing propylene oxide from large-scale industrial methanol | |
| CN105524027A (en) | Epoxypropane composition | |
| CN114956947B (en) | Separation method for preparing isopropylbenzene by hydrogenolysis of alpha, alpha-dimethylbenzyl alcohol | |
| CN112321378B (en) | Method for recycling waste liquid of co-production process of epoxypropane by co-oxidation method | |
| CN111892474B (en) | System and method for preprocessing cumene raw material of CHPPO device | |
| CN220223918U (en) | Device for reducing COD (chemical oxygen demand) of acidic water at top of catalytic fractionation tower |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20201013 |
|
| RJ01 | Rejection of invention patent application after publication |