CN111892474B - System and method for preprocessing cumene raw material of CHPPO device - Google Patents
System and method for preprocessing cumene raw material of CHPPO device Download PDFInfo
- Publication number
- CN111892474B CN111892474B CN202010676348.8A CN202010676348A CN111892474B CN 111892474 B CN111892474 B CN 111892474B CN 202010676348 A CN202010676348 A CN 202010676348A CN 111892474 B CN111892474 B CN 111892474B
- Authority
- CN
- China
- Prior art keywords
- collector
- phase
- cumene
- stirrer
- oil
- 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.)
- Active
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/10—Purification; Separation; Use of additives by extraction, i.e. purification or separation of liquid hydrocarbons with the aid of liquids
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a system and a method for preprocessing cumene raw materials of a CHPPO device, which mainly solve the problems of the prior art that the process is behind, the processing range is small and the operation cost is high. By adopting the system and the method, in a CHPPO device of 5-80 ten thousand tons/year, an alkali washing process of a stirrer, a first collector and a second collector is arranged, and the oil phase and the water phase in the discharge of the first collector are allowed to contain 1.0-6.0wt% of another water phase and an oil phase; the cumene containing 100-5000mg/kg of organic acid is subjected to alkaline washing pretreatment to obtain purified cumene with the organic acid less than or equal to 50mg/kg, the power consumption of a booster pump is saved by 6.3-145.1 kilowatts, the operation cost is saved by 17.67-25.43%, the problems are well solved, 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 preprocessing cumene raw materials of a CHPPO device.
Background
Propylene oxide PO is one of three large derivatives of propylene and is also an important basic chemical raw material. Most of epoxypropane is used for producing polyether polyol and then reacts with isocyanate to synthesize polyurethane, and the polyurethane is widely applied to the fields of automobiles, building energy conservation, refrigerator and freezer, elastomers, adhesives, coatings and the like, so that PO has good market application prospect. The propylene oxide PO production process technology is more, and mainly comprises the following three steps: chlorohydrin method, hydrogen peroxide direct oxidation HPPO method and indirect co-oxidation method. Wherein the chlorohydrin method mainly comprises the steps of transferring propylene and chlorine in the presence of waterForming chloropropanol, and then mixing the chloropropanol with excess Ca (OH) 2 Or NaOH is subjected to slurry saponification reaction, and HCl is removed to obtain propylene oxide, the method has the advantages of simple process and short flow, but a large amount of chlorine is consumed in the production process, a large amount of chlorine-containing sewage and waste residues are generated during saponification, three wastes are serious, and the environmental protection treatment cost is high. The hydrogen peroxide HPPO method mainly comprises the steps of H 2 O 2 The method has simple process route, but needs H to be used 2 O 2 Due to H 2 O 2 The price is relatively high, and the transportation is inconvenient, so H needs to be arranged at the same time 2 O 2 The device is matched with the device. The indirect co-oxidation method is mainly represented by a cumene co-oxidation CHPPO method, cumene hydroperoxide CHP is generated by the reaction of cumene and oxygen in the air, the CHP is then subjected to epoxidation reaction with propylene to generate propylene oxide PO and alpha, alpha-dimethylbenzyl alcohol DMBA, the alpha, alpha-dimethylbenzyl alcohol DMBA is dehydrated to generate alpha-methylstyrene, and the alpha-methylstyrene is hydrogenated to generate cumene for recycling. The method not only solves the problems of high material requirement and serious environmental pollution of the chlorohydrin method equipment, but also does not generate co-products to find the application market, and has been applied to a plurality of sets of industrial production devices in recent years. However, since the japanese sumitomo chemical company has a patent for the production technology and further development of CHPPO in China is limited to produce propylene oxide, a new process for producing propylene oxide by CHPPO method with independent intellectual property is required to be developed. In the development of the CHPPO method technology and the production of propylene oxide PO, in order to ensure that the reaction of cumene oxidation to cumene hydroperoxide CHP can be more rapid and effective, the cumene raw material needs to be pretreated to remove organic acid impurities below 50 mg/kg.
The invention patent application No. CN201910850055.4 in the prior art relates to a method for preparing cumene hydroperoxide by oxidizing cumene, which comprises the following steps: cumene hydroperoxide is prepared by oxidation of cumene in the presence of alpha-methylstyrene dimer. The process may also be carried out in the presence of a byproduct inhibitor as a preferred embodiment. When a certain amount of alpha-methylstyrene dimer is contained in the reaction liquid, the conversion rate of the isopropylbenzene is improved, and when the alpha-methylstyrene dimer and the byproduct inhibitor are added at the same time, the selectivity of the methyl phenyl ketone can be effectively reduced while the conversion rate of the isopropylbenzene is increased. The invention patent application number is CN201910528251.X agitator, including container seat and container, container threaded connection is on the container seat, the container has upper opening and lower opening, the upper opening is equipped with the container lid, lower opening and container seat threaded connection, the lower opening is equipped with the container end, be equipped with sealed pad between lower opening and the container end, be equipped with motor in the container seat, water tank and water pump, the top of container end is equipped with the stirring sword, the stirring sword is connected with the (mixing) shaft, the center of container end upwards protrudes and forms the fixing base, be connected with the motor after the (mixing) shaft runs through the container end, the (mixing) shaft overcoat has the bearing, the outer sleeve joint of bearing has the heat conduction cover, heat conduction cover interference fit is in the fixing base, be equipped with the annular chamber in the heat conduction cover, be equipped with the inlet opening between inlet port and the annular chamber, the water pump intercommunication has drinking-water pipe and inlet tube, the drinking-water pipe communicates with the water tank, inlet tube and annular chamber intercommunication, be equipped with the check valve on the inlet tube, thereby make the agitator can continuous operation, the practicality is strong. The invention patent application number is CN201110445155.2 a method for recycling ethylene gas from tail gas and a water alkali washing tower thereof, and discloses a method for recycling ethylene gas from tail gas, wherein tail gas from a buffer tank (1) enters a lower section through a gas inlet (14), enters a middle section through a bypass gas pipe (8) after exchange absorption with water, enters an upper section through a bypass gas pipe (9) after exchange absorption with alkali liquor with concentration of 1-3% in the section, exchanges absorption with water again, and is purified and then is sent to a gas cabinet (7) from a gas outlet (15); water from the water circulation tank (3) enters the upper section through the water inlet (16) at first, enters the lower section through the bypass water pipe (10) after exchange absorption is completed, and returns to the water circulation tank (3) from the water outlet (17) after exchange absorption is completed; 1-3% alkali liquor with the concentration from the alkali liquor circulation tank (5) enters the middle section from the alkali liquor inlet (18), and returns to the alkali liquor circulation tank (5) from the alkali liquor outlet (19) after exchange absorption is completed; the method can increase the ethylene gas content from 89.5% to 96.43%, and the VAC content is reduced from 9.49% to 2.57%.
The invention patent application number of the prior art is CN201910850055.4, which discloses a method for preparing cumene hydroperoxide by oxidizing cumene, only the technical scheme for preparing cumene hydroperoxide is disclosed, and the technical method for pretreating the cumene raw material of a CHPPO device to remove organic acid impurities is not involved. The invention patent application number is CN201910528251.X stirrer, only the operation function of a single device is disclosed, and the technical steps of connecting the whole process flow to pretreat the alkaline eluting and removing organic acid impurities in the cumene raw material of the CHPPO device are not involved. The invention patent application number is CN201110445155.2, a method for recovering ethylene gas from tail gas and a water-alkali washing tower thereof only disclose the technical means of pretreatment of ethylene gas by adopting the alkali washing tower/water washing tower with large equipment engineering investment and high operation and running cost, and the purification treatment range is only 200-1000
mg/kg. Therefore, the prior art has the problems of laggard process level, small purification treatment range and high operation and running cost in the process of pretreating the acid-containing cumene raw material by a CHPPO device.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides a system and a method for preprocessing cumene raw materials of a CHPPO device, so that the technical level of the process is further improved, the purification treatment range is enlarged, and the operation cost is reduced.
In order to achieve the above purpose, the present invention adopts the following technical scheme:
the first aspect of the invention provides a system for preprocessing cumene raw material of a CHPPO device, which comprises a stirrer, a first collector and a second collector;
wherein, the top of the stirrer is provided with a feed pipe containing acid cumene and fresh alkali liquor, and the bottom is provided with a discharge pipe which is communicated with the first collector;
the top of the first collector is provided with an oil phase discharging pipe, and the bottom of the first collector is provided with an aqueous phase discharging pipe; the oil phase discharging pipe and the water phase discharging pipe are communicated with the second concentrator;
the second collector is provided with a cumene purifying discharge pipeline and a waste alkali liquid discharge pipeline;
the discharge pipe, the oil phase discharge pipe and the water phase discharge pipe are respectively provided with a stirrer kettle liquid pump, an oil phase booster pump and a water phase booster pump.
Further, the stirring impeller arranged in the stirrer is one of a propelling impeller, a disc impeller, a hinged blade impeller, an inclined blade turbine, a long thin blade propeller, an open straight blade turbine, a disc straight blade turbine, a backward bent impeller and a plate frame blade impeller.
Further, the first collector contains three layers of special materials, and sequentially consists of oleophilic and hydrophobic materials, wherein the oleophilic and hydrophobic materials are one of glass fiber, PET hollow fiber, PP hollow fiber and oil-absorbing cotton fiber; the oleophobic hydrophilic material is modified fiber, composite fiber and TiO 2 A material of nano fiber and absorbent cotton fiber.
Further, the second collector contains three layers of special materials, and sequentially consists of oleophilic and hydrophobic materials, wherein the oleophilic and hydrophobic material is one of glass fiber, PET hollow fiber, PP hollow fiber and oil-absorbing cotton fiber; the oleophobic hydrophilic material is modified fiber, composite fiber and TiO 2 A material of nano fiber and absorbent cotton fiber.
The second aspect of the invention provides a method for pretreating cumene raw material of a CHPPO device by adopting the system, which comprises the following process flows in a large-scale commercial CHPPO industrial production device with nominal capacity of 5-80 ten thousand tons/year:
a) Introducing acid-containing isopropylbenzene containing organic acid impurities from outside the world into a stirrer, introducing fresh alkali liquor from outside the world into the stirrer, and carrying out flow segmentation, liquid drop dispersion, liquid-liquid contact, axial mixing, radial mixing, mixing diffusion and oil-water combination on the acid-containing isopropylbenzene and the fresh alkali liquor in the stirrer to carry out neutralization reaction on the organic acid impurities in the acid-containing isopropylbenzene containing the organic acid impurities so as to remove the organic acid impurities;
b) The stirrer discharge material flowing out of the stirrer enters a first collector containing three layers of special materials after being pressurized by a stirrer kettle liquid pump; the method comprises the steps of collecting tiny oil drop particles in a first collector by utilizing the characteristics of oleophylic and hydrophobic materials to form a continuous oil phase, and collecting tiny water drop particles by utilizing the characteristics of oleophylic and hydrophilic materials to form a continuous water phase, so that first oil-water layering separation is realized; the first aqueous phase exiting the first aggregator is allowed to contain a small amount of aqueous phase, and the first aqueous phase exiting the first aggregator is also allowed to contain a small amount of oil phase;
c) The oil phase flowing out of the first collector is pressurized by the oil phase booster pump and then enters the second collector; the water phase flowing out of the first collector is pressurized by the water phase booster pump and then enters the second collector; the oil-water phase aggregation device comprises a first aggregation device, a second aggregation device and a third aggregation device, wherein the first aggregation device is used for aggregating tiny oil drop particles to form a continuous oil phase by utilizing the characteristics of oleophilic hydrophobic materials, and meanwhile, the tiny water drop particles are aggregated to form a continuous water phase by utilizing the characteristics of oleophobic hydrophilic materials, so that the second oil-water layer separation is realized; the oil phase of the second concentrator does not allow an aqueous phase, which is sent out of the boundary as clean cumene; the aqueous phase of the second accumulator also does not allow an oil phase to be contained, which is also sent out as spent lye.
Further, ethylbenzene in acid-containing cumene from the outside of the world contains organic acid impurities is less than or equal to 0.60wt%, propylbenzene is less than or equal to 0.30wt%, ding Ben is 0.10wt%, and the content of the organic acid impurities is 100-5000mg/kg.
It is further preferred that ethylbenzene in acid-containing cumene from the outside of the world contains organic acid impurities is less than or equal to 0.10 wt.%, cumene is less than or equal to 0.05 wt.%, ding Ben is 0.03 wt.%, and the organic acid impurity content is 200-2000mg/kg.
More preferably, ethylbenzene in acid-containing cumene from the outside of the world contains organic acid impurities is less than or equal to 0.01wt%, propylbenzene is less than or equal to 0.01wt%, ding Ben is 0.01wt%, and the content of the organic acid impurities is 500-1000mg/kg.
Further, the operating pressure of the stirrer is 0.50-1.10MPaA, the operating temperature is 25-85 ℃, and the rotating speed of the impeller of the stirrer is 20-2000RPM; the first accumulator is operated at a pressure of 0.50 to 1.10MPaA and at a temperature of 25 to 85 ℃, the accumulator oil phase comprises 1.0 to 6.0wt% of the aqueous phase, and the accumulator water phase comprises 1.0 to 6.0wt% of the oil phase; the second accumulator operates at a pressure of 0.50-1.10MPaA and an operating temperature of 25-85 ℃; the inlet operation pressure of a liquid pump of the stirrer kettle is 0.50-1.10MPaA, the outlet operation pressure is 0.70-1.30MPaA, and the operation temperature is 25-85 ℃; the oil phase booster pump has an inlet operation pressure of 0.45-1.05MPaA, an outlet operation pressure of 0.65-1.25MPaA and an operation temperature of 25-85 ℃; the inlet operation pressure of the water phase booster pump is 0.50-1.10MPaA, the outlet operation pressure is 0.70-1.30MPaA, and the operation temperature is 25-85 ℃.
Further preferably, the agitator operates at a pressure of 0.60-1.00MPaA, an operating temperature of 35-75deg.C, and a rotational speed of the agitator impeller of 60-1000RPM; the first accumulator is operated at a pressure of 0.60 to 1.00MPaA and at a temperature of 35 to 75 ℃, the accumulator oil phase comprises 2.0 to 5.5wt% of the aqueous phase, and the accumulator water phase comprises 2.0 to 5.5wt% of the oil phase; the second accumulator operates at a pressure of 0.60-1.00MPaA and an operating temperature of 35-75deg.C; the inlet operation pressure of a liquid pump of the stirrer kettle is 0.60-1.00MPaA, the outlet operation pressure is 0.80-1.20MPaA, and the operation temperature is 35-75 ℃; the oil phase booster pump has an inlet operation pressure of 0.55-0.95MPaA, an outlet operation pressure of 0.75-1.15MPaA and an operation temperature of 35-75 ℃; the inlet operation pressure of the water phase booster pump is 0.60-1.00MPaA, the outlet operation pressure is 0.80-1.20MPaA, and the operation temperature is 35-75 ℃.
More preferably, the agitator operating pressure is 0.70-0.90MPaA, the operating temperature is 45-65 ℃, and the rotational speed of the agitator impeller is 200-600RPM; the first accumulator is operated at a pressure of 0.70-0.90MPaA and at a temperature of 45-65deg.C, the accumulator oil phase contains 2.5-4.5wt% of the aqueous phase, and the accumulator water phase contains 2.5-4.5wt% of the oil phase; the second collector operates at a pressure of 0.70-0.90MPaA and an operating temperature of 45-65 ℃; the inlet operation pressure of a liquid pump of the stirrer kettle is 0.70-0.90MPaA, the outlet operation pressure is 0.90-1.10MPaA, and the operation temperature is 45-65 ℃; the oil phase booster pump has an inlet operation pressure of 0.65-0.85MPaA, an outlet operation pressure of 0.85-1.05MPaA and an operation temperature of 45-65 ℃; the inlet operation pressure of the water phase booster pump is 0.70-0.90MPaA, the outlet operation pressure is 0.90-1.10MPaA, and the operation temperature is 45-65 ℃.
Compared with the prior art, the invention has the following technical effects:
the invention relates to a system and a method for preprocessing cumene raw materials of a CHPPO device, which are characterized in that for a large-scale commercial CHPPO industrial production device with nominal capacity of 5-80 ten thousand tons per year, an alkaline washing process flow of a stirrer-first collector-second collector is adopted to replace a process flow of an alkaline washing tower in the prior art, and an oil phase and a water phase in discharge of the first collector are set to allow to contain 1.0-6.0wt% of another water phase and oil phase; the cumene raw material from the outside of the world containing 100-5000mg/kg of organic acid impurities is subjected to alkaline washing pretreatment to remove the organic acid impurities, so that purified cumene with the organic acid impurity content less than or equal to 50mg/kg is obtained, the power consumption of a booster pump can be saved by 6.3-145.1 kilowatts, the operation cost is saved by 17.67-25.43%, and a better technical effect is obtained.
Drawings
FIG. 1 is a schematic process flow diagram of a cumene feed pretreatment process;
wherein, the A-stirrer, the B-stirrer kettle liquid pump, the C-first collector, the D-oil phase booster pump, the E-water phase booster pump, the F-second collector, the 11-acid-containing isopropylbenzene, the 12-stirrer discharging, the 13-oil phase polymerization, the 14-purifying isopropylbenzene, the 21-fresh alkali liquor, the 22-water phase polymerization and the 23-waste alkali liquor;
the process flow of the invention is described as follows:
the acid-containing cumene 11 from the impurities of the organic acid outside the boundary enters a stirrer A, fresh alkali liquor 21 from the outside of the boundary also enters the stirrer A, oil-water mixture is stirred and mixed, discharged material 12 of the stirrer enters a first collector C after being pressurized by a stirrer kettle pump B, the discharged material is subjected to first aggregation and separation, discharged material 13 enters a second collector F after being pressurized by an oil phase booster pump D, discharged material 22 enters the second collector F after being pressurized by an aqueous phase booster pump F, the discharged material 13 and the discharged material 22 are in the second collector F after being subjected to second aggregation and separation, discharged material 14 is discharged outside the boundary as purified cumene, and discharged material 23 is discharged outside the boundary.
Detailed Description
The invention provides a system and a method for preprocessing cumene raw materials of a CHPPO device. The present invention will be described in detail and in detail by way of the following examples, which are not intended to limit the scope of the invention, for better understanding of the invention.
Comparative example 1
In the prior art, the acid-containing isopropylbenzene raw material is subjected to alkaline washing by adopting a conventional alkaline washing tower process flow, the nominal capacity of a CHPPO device is 5 ten thousand tons/year of a commercial industrial production device, the equipment parameters of a main equipment alkaline washing tower are phi 3000 multiplied by 38000mm, and the power consumption of a circulating alkaline liquid pump is 35.7 kilowatts. The content of organic acid impurities in acid-containing cumene outside the boundary is 200-1000mg/kg, and after alkaline washing treatment of fresh alkaline liquor and circulating alkaline liquor in an alkaline washing tower in the prior art, purified cumene with the content of organic acid impurities being less than or equal to 50mg/kg is obtained, and other process data are shown in Table 1.
[ example 1 ]
As shown in fig. 1, the embodiment provides a method for pretreating cumene raw material of a CHPPO device, which specifically comprises the following process flows: the acid-containing cumene 11 from the impurities of the organic acid outside the boundary enters a stirrer A, fresh alkali liquor 21 from the outside of the boundary also enters the stirrer A, oil-water mixture is stirred and mixed, discharged material 12 of the stirrer enters a first collector C after being pressurized by a stirrer kettle pump B, the discharged material is subjected to first aggregation and separation, discharged material 13 enters a second collector F after being pressurized by an oil phase booster pump D, discharged material 22 enters the second collector F after being pressurized by an aqueous phase booster pump F, the discharged material 13 and the discharged material 22 are in the second collector F after being subjected to second aggregation and separation, discharged material 14 is discharged outside the boundary as purified cumene, and discharged material 23 is discharged outside the boundary.
In the commercial industrial production device with the nominal capacity of 5 ten thousand tons/year, the structure type of the stirrer impeller in main equipment is a disc impeller, the rotating speed of the stirrer impeller is 60RPM, and the specification phi of the stirrer equipment is 1000 multiplied by 2800 mm; the oleophilic and hydrophobic material of the first collector is glass fiber, and the oleophobic and hydrophilic material of the first collector is TiO 2 Nanofibers, first collector specification Φ3000×11500 millimeters; the oleophilic and hydrophobic material of the second concentrator is PET hollow fiber, the oleophobic and hydrophilic material of the second concentrator is modified fiber, and the specification phi of the second concentrator is 3000 multiplied by 11500 mm; the power consumption of the booster pump is 29.4 kilowatts. The purified cumene with the organic acid impurity content of less than or equal to 50mg/kg is obtained after the pretreatment of the alkaline washing process of the stirrer-first collector-second collector in the embodiment, wherein the organic acid impurity content in the acid cumene is 2000mg/kg, and other process data are shown in Table 2. And [ comparative example 1 ]Compared with the prior art, the electric consumption of the booster pump can be saved by 6.3 kilowatts, the operation cost is saved by 17.67%, and a better technical effect is achieved.
Comparative example 2
In the prior art, the acid-containing isopropylbenzene raw material is subjected to alkaline washing by adopting a conventional alkaline washing tower process flow, the nominal capacity of a CHPPO device is 10 ten thousand tons/year of a commercial industrial production device, the equipment parameters of a main equipment alkaline washing tower are phi 4400 multiplied by 40000mm, and the power consumption of a circulating alkaline liquid pump is 71.3 kilowatts. The content of organic acid impurities in acid-containing cumene outside the boundary is 200-1000mg/kg, and after alkaline washing treatment of fresh alkaline liquor and circulating alkaline liquor in an alkaline washing tower in the prior art, purified cumene with the content of organic acid impurities being less than or equal to 50mg/kg is obtained, and other process data are shown in Table 1.
[ example 2 ]
Similarly [ example 1 ], the nominal capacity of the CHPPO device is changed into a commercial industrial production device of 10 ten thousand tons/year, the structural style of the stirrer impeller in the main equipment is a backward bending impeller, the rotating speed of the stirrer impeller is 120RPM, and the specification phi 1400 multiplied by 3000 mm of the stirrer equipment; the oleophobic and hydrophobic material of the first collector is PET hollow fiber glass fiber, the oleophobic and hydrophilic material of the first collector is modified fiber, and the specification phi of the first collector is 4600 multiplied by 12200 mm; the oleophilic and hydrophobic material of the second concentrator is glass fiber, the oleophobic and hydrophilic material of the second concentrator is composite fiber, and the specification phi of the second concentrator is 4600 multiplied by 12200 mm; the power consumption of the booster pump is 57.0 kilowatts. The content of organic acid impurity from the acid cumene outside the boundary is 180mg/kg, and after the pretreatment by the alkaline washing process of the stirrer-first collector-second collector in the embodiment, the purified cumene with the content of organic acid impurity being less than or equal to 50mg/kg is obtained, and other process data are shown in Table 2. Compared with the method of the comparative example 2, the method can save 14.3 kilowatts of power consumption of the booster pump and 20.09 percent of operation cost, and achieves better technical effect.
[ comparative example 3 ]
In the prior art, the acid-containing isopropylbenzene raw material is subjected to alkaline washing by adopting a conventional alkaline washing tower process flow, the nominal capacity of a CHPPO device is 20 ten thousand tons/year of a commercial industrial production device, the equipment parameters of a main equipment alkaline washing tower are phi 6000 multiplied by 44000mm, and the power consumption of a circulating alkaline liquid pump is 142.7 kilowatts. The content of organic acid impurities in acid-containing cumene outside the boundary is 200-1000mg/kg, and after alkaline washing treatment of fresh alkaline liquor and circulating alkaline liquor in an alkaline washing tower in the prior art, purified cumene with the content of organic acid impurities being less than or equal to 50mg/kg is obtained, and other process data are shown in Table 1.
[ example 3 ]
Similarly to example 1, only the nominal capacity of the CHPPO device is changed to a commercial industrial production device of 20 ten thousand tons/year, the structural style of the stirrer impeller in the main equipment is a oblique blade turbine, the rotating speed of the stirrer impeller is 240RPM, and the specification phi 2000 x 3200 mm of the stirrer equipment; the oleophobic and hydrophobic material of the first collector is glass fiber, the oleophobic and hydrophilic material of the first collector is composite fiber, and the specification phi of the first collector is 6800 multiplied by 13400 mm; the oleophilic and hydrophobic material of the second collector is oil-absorbing cotton fiber, and the oleophobic and hydrophilic material of the second collector is TiO 2 Nanofibers, second concentrator specification Φ6800×13400 millimeters; the power consumption of the booster pump is 110.0 kilowatts. The organic acid impurity content from the acid cumene outside the boundary is 3300mg/kg, and after the pretreatment by the alkaline washing process of the stirrer-first collector-second collector in this example, purified cumene with the organic acid impurity content less than or equal to 50mg/kg is obtained, and other process data are shown in Table 2. Compared with the method of the comparative example 3, the method can save 32.7 kilowatts of power consumption of the booster pump and 22.89 percent of operation cost, and achieves better technical effect.
[ comparative example 4 ]
In the prior art, the acid-containing isopropylbenzene raw material is subjected to alkaline washing by adopting a conventional alkaline washing tower process flow, the nominal capacity of a CHPPO device is 40 ten thousand tons/year of a commercial industrial production device, the equipment parameters of a main equipment alkaline washing tower are phi 8800 multiplied by 46000mm, and the power consumption of a circulating alkaline liquid pump is 285.3 kilowatts. The content of organic acid impurities in acid-containing cumene outside the boundary is 200-1000mg/kg, and after alkaline washing treatment of fresh alkaline liquor and circulating alkaline liquor in an alkaline washing tower in the prior art, purified cumene with the content of organic acid impurities being less than or equal to 50mg/kg is obtained, and other process data are shown in Table 1.
[ example 4 ]
As in example 1, only the CHPPO unit is nominalThe capacity is changed into a commercial industrial production device with 40 ten thousand tons/year, the structural style of a stirrer impeller in main equipment is a long thin blade propeller, the rotating speed of the stirrer impeller is 20RPM, and the specification phi 2800 multiplied by 3400 mm of the stirrer equipment; the oleophilic and hydrophobic material of the first collector is oil-absorbing cotton fiber, and the oleophobic and hydrophilic material of the first collector is TiO 2 Nanofibers, first collector specification Φ10000×14200 millimeters; the oleophilic and hydrophobic material of the second concentrator is PP hollow fiber, the oleophobic and hydrophilic material of the second concentrator is absorbent cotton fiber, and the specification phi of the second concentrator is 10000 multiplied by 14200 mm; the power consumption of the booster pump is 222.3 kilowatts. The content of organic acid impurity from the acid cumene outside the boundary is 100mg/kg, and after the pretreatment by the alkaline washing process of the stirrer-first collector-second collector in this example, purified cumene with the content of organic acid impurity less than or equal to 50mg/kg is obtained, and other process data are shown in Table 2. Compared with the method of the comparative example 4, the method can save 63.0 kilowatts of power consumption of the booster pump and 22.08 percent of operation cost, and achieves better technical effect.
Comparative example 5
In the prior art, the acid-containing isopropylbenzene raw material is subjected to alkaline washing by adopting a conventional alkaline washing tower process flow, the nominal capacity of a CHPPO device is 40 ten thousand tons/year of a commercial industrial production device, the equipment parameters of a main equipment alkaline washing tower are phi 8400 multiplied by 46000mm, and the power consumption of a circulating alkaline liquid pump is 285.3 kilowatts. The content of organic acid impurities in acid-containing cumene outside the boundary is 200-1000mg/kg, and after alkaline washing treatment of fresh alkaline liquor and circulating alkaline liquor in an alkaline washing tower in the prior art, purified cumene with the content of organic acid impurities being less than or equal to 50mg/kg is obtained, and other process data are shown in Table 1.
[ example 5 ]
Similarly [ example 1 ], the nominal capacity of the CHPPO device is changed into 40 ten thousand tons/year commercial industrial production device, the structural style of the stirrer impeller in the main equipment is a push-type impeller, the rotating speed of the stirrer impeller is 2000RPM, and the specification phi 2800 multiplied by 3400 mm of the stirrer equipment; the oleophilic and hydrophobic material of the first collector is PP hollow fiber, the oleophobic and hydrophilic material of the first collector is absorbent cotton fiber, and the specification phi of the first collector is 10000 multiplied by 14000 mm; the oleophilic and hydrophobic material of the second collector is oil-absorbing cotton fiber, the oleophobic and hydrophilic material of the second collector is absorbent cotton fiber, and the specification phi of the second collector is 10000 multiplied by 14000 mm; the power consumption of the booster pump is 219.2 kilowatts. The organic acid impurity content from the acid cumene outside the boundary is 5000mg/kg, and after the pretreatment by the alkaline washing process of the stirrer-first collector-second collector in this example, purified cumene with the organic acid impurity content less than or equal to 50mg/kg is obtained, and other process data are shown in Table 2. Compared with the method of the comparative example 5, the method can save 66.1 kilowatts of power consumption of the booster pump and 23.17 percent of operation cost, and achieves better technical effect.
[ comparative example 6 ]
In the prior art, the acid-containing isopropylbenzene raw material is subjected to alkaline washing by adopting a conventional alkaline washing tower process flow, the nominal capacity of a CHPPO device is 80 ten thousand tons/year of a commercial industrial production device, the equipment parameters of a main equipment alkaline washing tower are phi 12000 multiplied by 50000mm, and the power consumption of a circulating alkaline liquid pump is 570.7 kilowatts. The content of organic acid impurities in acid-containing cumene outside the boundary is 200-1000mg/kg, and after alkaline washing treatment of fresh alkaline liquor and circulating alkaline liquor in an alkaline washing tower in the prior art, purified cumene with the content of organic acid impurities being less than or equal to 50mg/kg is obtained, and other process data are shown in Table 1.
[ example 6 ]
In the same way as in the example 1, only the nominal capacity of the CHPPO device is changed to 80 ten thousand tons/year commercial industrial production device, the structural style of the stirrer impeller in the main equipment is an open straight blade turbine, the rotating speed of the stirrer impeller is 1000RPM, and the specification phi 3800 multiplied by 4000mm of the stirrer equipment; the oleophilic and hydrophobic material of the first collector is oil-absorbing cotton fiber, the oleophobic and hydrophilic material of the first collector is composite fiber, and the specification phi of the first collector is 15200 multiplied by 15400 millimeters; the oleophilic and hydrophobic material of the second collector is PP hollow fiber, and the oleophobic and hydrophilic material of the second collector is TiO 2 Nanofibers, second concentrator specification Φ15200×15400 millimeters; the power consumption of the booster pump is 425.5 kilowatts. The content of organic acid impurity from the acid cumene outside the boundary is 420mg/kg, and after the pretreatment by the alkaline washing process of the stirrer-first collector-second collector in this example, purified cumene with the content of organic acid impurity less than or equal to 50mg/kg is obtained, and other process data are shown in Table 2. And [ toCompared with the proportion 6, the electric consumption of the booster pump can be saved by 145.1 kilowatts, the operation cost is saved by 25.43 percent, and a better technical effect is achieved.
TABLE 1 prior art caustic tower Process data List
TABLE 2 list of major plant Process data for the invention
The above description of the specific embodiments of the present invention has been given by way of example only, and the present invention is not limited to the above described specific embodiments. It will be apparent to those skilled in the art that any equivalent modifications and substitutions of the present invention are intended to be within the scope of the present invention. Accordingly, equivalent changes and modifications are intended to be included within the scope of the present invention without departing from the spirit and scope thereof.
Claims (4)
1. A method for pretreating cumene raw material of a CHPPO device is characterized by comprising the following process flows in a large-scale commercial CHPPO industrial production device with nominal capacity of 5-80 ten thousand tons/year:
a) Acid-containing cumene (11) from an off-boundary organic acid impurity enters a stirrer (A), and fresh lye (21) from an off-boundary also enters the stirrer (A); in the stirrer (A), the acid-containing cumene (11) and the fresh alkali liquor (21) are subjected to flow segmentation, liquid drop dispersion, liquid-liquid contact, axial mixing, radial mixing, mixing diffusion and oil-water combination, and the organic acid impurities in the acid-containing cumene (11) containing the organic acid impurities and the fresh alkali liquor (21) undergo neutralization reaction to be removed;
b) The stirrer discharging material (12) flowing out of the stirrer (A) enters a first collector (C) containing three layers of special materials after being pressurized by a stirrer kettle liquid pump (B); in the first collector (C), the characteristics of the oleophilic and hydrophobic materials are utilized to aggregate the tiny oil drop particles to form a continuous oil phase, and meanwhile, the characteristics of the oleophobic and hydrophilic materials are utilized to aggregate the tiny water drop particles to form a continuous water phase, so that the first oil-water layering separation is realized; the first collector (C) effluent of a first phase (13) of polymeric phase allows a small amount of aqueous phase, and the first collector (C) effluent of a first phase (22) of polymeric phase also allows a small amount of oily phase;
c) An oil phase accumulating phase (13) flowing out of the first collector (C) enters the second collector (F) after being pressurized by an oil phase booster pump (D); a water-phase polymer (22) flowing out of the first collector (C) is pressurized by a water-phase booster pump (E) and then enters the second collector (F); the oil-water phase aggregation device comprises an oil-water phase aggregation device, a first aggregation device, a second aggregation device and a third aggregation device, wherein the oil-water phase aggregation device comprises an oil-water phase aggregation device (13) and a water-water phase aggregation device (22), wherein the oil-water phase aggregation device comprises a first aggregation device (F) and a second aggregation device (F) which are arranged in the first aggregation device, the second aggregation device is arranged in the second aggregation device, the first aggregation device is arranged in the first aggregation device, the second aggregation device is arranged in the second aggregation device, and the third aggregation device is arranged in the second aggregation device; the oil phase of the second accumulator (F) does not allow an aqueous phase, which is sent out as purge cumene (14); the aqueous phase of the second collector (F) also does not allow an oily phase to be contained, which is also sent out as spent lye (23);
the system for preprocessing the cumene raw material by the CHPPO device adopted by the method comprises a stirrer (A), a first collector (C) and a second collector (F);
wherein, the top of the stirrer (A) is provided with a feed pipe containing acid cumene (11) and fresh alkali liquor (21), and the bottom is provided with a discharge pipe which is communicated with the first collector (C);
an oil phase discharging pipe is arranged at the top of the first collector (C), and an aqueous phase discharging pipe is arranged at the bottom of the first collector (C); the oil phase discharging pipe and the water phase discharging pipe are communicated with the second collector (F);
the second collector (F) is provided with a purified isopropylbenzene (14) discharging pipeline and a waste alkali liquid (23) discharging pipeline;
the stirrer kettle liquid pump (B), the oil phase booster pump (D) and the water phase booster pump (E) are respectively arranged on the discharge pipe, the oil phase discharge pipe and the water phase discharge pipe;
ethylbenzene in acid-containing cumene (11) containing organic acid impurities from outside the world is less than or equal to 0.60 and wt percent, cumene is less than or equal to 0.30 and wt percent, ding Ben and 3534.10 and wt percent, and the content of the organic acid impurities is 100-5000 mg/kg;
the method for preprocessing the cumene raw material of the CHPPO device is characterized in that the operating pressure of the stirrer (A) is 0.50-1.10MPaA, the operating temperature is 25-85 ℃, and the rotating speed of an impeller of the stirrer is 20-2000RPM; the operating pressure of the first collector (C) is 0.50-1.10MPaA, the operating temperature is 25-85 ℃, the oil phase of the collector contains 1.0-6.0wt% of water phase, and the water phase of the collector contains 1.0-6.0wt% of oil phase; the second accumulator (F) is operated at a pressure of 0.50-1.10MPaA and at a temperature of 25-85 ℃; the inlet operation pressure of the stirrer kettle liquid pump (B) is 0.50-1.10MPaA, the outlet operation pressure is 0.70-1.30MPaA, and the operation temperature is 25-85 ℃; the oil phase booster pump (D) has an inlet operation pressure of 0.45-1.05MPaA, an outlet operation pressure of 0.65-1.25MPaA and an operation temperature of 25-85 ℃; the inlet operation pressure of the water phase booster pump (E) is 0.50-1.10MPaA, the outlet operation pressure is 0.70-1.30MPaA, and the operation temperature is 25-85 ℃;
the first collector (C) contains three layers of special materials, and sequentially consists of oleophilic and hydrophobic materials, oleophobic and hydrophilic materials, wherein the oleophilic and hydrophobic materials are one of glass fibers, PET hollow fibers, PP hollow fibers and oil-absorbing cotton fibers; the oleophobic hydrophilic material is modified fiber, composite fiber and TiO 2 Nano fiber,One material of absorbent cotton fiber;
the second collector (F) contains three layers of special materials, and sequentially consists of oleophilic and hydrophobic materials, oleophobic and hydrophilic materials and oleophilic and hydrophobic materials, wherein the oleophilic and hydrophobic materials are one of glass fibers, PET hollow fibers, PP hollow fibers and oil-absorbing cotton fibers; the oleophobic hydrophilic material is modified fiber, composite fiber and TiO 2 A material of nano fiber and absorbent cotton fiber.
2. The method for pretreating cumene raw material of a CHPPO device according to claim 1, wherein ethylbenzene in the acid-containing cumene (11) containing organic acid impurities from outside the world is not more than 0.01wt%, propylbenzene is not more than 0.01wt%, ding Ben 0.01.01 wt%, and the organic acid impurity content is 200-2000mg/kg.
3. The method for pretreatment of cumene feed to a CHPPO unit according to claim 1, wherein the operation pressure of the stirrer (a) is 0.70-0.90mpa, the operation temperature is 45-65 ℃, and the rotation speed of the stirrer impeller is 200-600RPM; the operating pressure of the first collector (C) is 0.70-0.90MPaA, the operating temperature is 45-65 ℃, the oil phase of the collector contains 2.5-4.5wt% of water phase, and the water phase of the collector contains 2.5-4.5wt% of oil phase; the second accumulator (F) is operated at a pressure of 0.70-0.90MPaA and at a temperature of 45-65 ℃; the inlet operation pressure of the stirrer kettle liquid pump (B) is 0.70-0.90MPaA, the outlet operation pressure is 0.90-1.10MPaA, and the operation temperature is 45-65 ℃; the oil phase booster pump (D) has an inlet operation pressure of 0.65-0.85MPaA, an outlet operation pressure of 0.85-1.05MPaA and an operation temperature of 45-65 ℃; the inlet operation pressure of the water phase booster pump (E) is 0.70-0.90MPaA, the outlet operation pressure is 0.90-1.10MPaA, and the operation temperature is 45-65 ℃.
4. The method for pretreating cumene raw material of a CHPPO device according to claim 1, wherein the stirring impeller structure type arranged in the stirrer (a) is one of a push impeller, a disc impeller, a hinge impeller, a diagonal blade turbine, a long thin blade propeller, an open straight blade turbine, a disc straight blade turbine, a backward bent impeller and a plate-and-frame impeller.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010676348.8A CN111892474B (en) | 2020-07-14 | 2020-07-14 | System and method for preprocessing cumene raw material of CHPPO device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010676348.8A CN111892474B (en) | 2020-07-14 | 2020-07-14 | System and method for preprocessing cumene raw material of CHPPO device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN111892474A CN111892474A (en) | 2020-11-06 |
| CN111892474B true CN111892474B (en) | 2023-08-01 |
Family
ID=73192695
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010676348.8A Active CN111892474B (en) | 2020-07-14 | 2020-07-14 | System and method for preprocessing cumene raw material of CHPPO device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111892474B (en) |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101100413A (en) * | 2006-07-04 | 2008-01-09 | 中国石油化工集团公司 | Method for removing alkali and water in cyclonexane oxidative liquid |
| CN202322668U (en) * | 2011-11-08 | 2012-07-11 | 太仓塑料助剂厂有限公司 | Continuous alkali wash system for isopropylbenzene |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ES2635108T3 (en) * | 2013-02-26 | 2017-10-02 | Borealis Ag | Process to purify hydrocarbons |
-
2020
- 2020-07-14 CN CN202010676348.8A patent/CN111892474B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101100413A (en) * | 2006-07-04 | 2008-01-09 | 中国石油化工集团公司 | Method for removing alkali and water in cyclonexane oxidative liquid |
| CN202322668U (en) * | 2011-11-08 | 2012-07-11 | 太仓塑料助剂厂有限公司 | Continuous alkali wash system for isopropylbenzene |
Non-Patent Citations (2)
| Title |
|---|
| 孙李宏主编.船舶管理 知识点解析.《船舶管理 知识点解析》.大连海事大学出版社,2014,第108页. * |
| 胡邦喜编著.液压润滑系统的清洁度控制.《液压润滑系统的清洁度控制》.2003,第137-139页. * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN111892474A (en) | 2020-11-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104759249B (en) | The recoverying and utilizing method and its active residue of a kind of catalytic coal gasifaction lime-ash | |
| CN111848325B (en) | Method and system for alkaline washing of cumene raw material by CHPPO device | |
| EP3865461A1 (en) | Method for treating production wastewater from preparation of propylene oxide with co-oxidation method | |
| CN1989292A (en) | Method for black liquor treatment | |
| CN107537293A (en) | A kind of closed cycle bacterial desulfurization and the method for reclaiming elemental sulfur | |
| CN1439599A (en) | Production for stable chlorinedioxide solution | |
| CN111892474B (en) | System and method for preprocessing cumene raw material of CHPPO device | |
| CN109970511B (en) | Method for synthesizing 1, 3-propylene glycol by resource utilization of HPPO byproduct | |
| CN108383335B (en) | High-concentration organic wastewater treatment system and method | |
| CN111807920A (en) | Method and system for deacidifying cumene raw material of CHPPO (chlorinated Polypropylene oxide) device | |
| CN217202410U (en) | Reclaimed water recycling system | |
| CN1103749C (en) | Treatment of effluent streams containing organic acids | |
| CN109160660B (en) | Method for recovering glycolic acid from sodium carboxymethylcellulose production wastewater | |
| CN101328158B (en) | Method for synthesizing butyl oxide linkage | |
| CN212894326U (en) | Wet oxidation reaction system for water treatment | |
| CN113292191A (en) | Residual oil catalytic pyrolysis and coal-to-olefin waste alkali liquor resource utilization device | |
| CN1227198C (en) | Method for preparing relevant alcohol and ketone by adding hydrogen into hydroperoxide of hydrocarbon | |
| CN102153223A (en) | Sodium carboxymethylcellulose industrial sewage recycling device | |
| CN113289468A (en) | Treatment device for silicon tetrachloride tail gas | |
| CN208038241U (en) | A kind of biogas hydrogen manufacturing circulatory system of PTA sewage disposals | |
| CN111392978A (en) | Landfill leachate sludge reduction synergistic concentrated solution recycling treatment process | |
| CN107032554A (en) | A kind of alkali decrement waste water dual treatment method and apparatus | |
| CN214936760U (en) | Residual oil catalytic thermal cracking and coal-to-olefin waste alkali liquor resource utilization device | |
| CN107501206A (en) | Solvent purifications method rubber accelerator M synthesis sulfenamide type accelerators TBBS method | |
| CN114572993B (en) | Method and device for refining potassium fluoborate as byproduct in synthesis of medical intermediate |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |