CN111848325B - Method and system for alkaline washing of cumene raw material by CHPPO device - Google Patents

Method and system for alkaline washing of cumene raw material by CHPPO device Download PDF

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CN111848325B
CN111848325B CN202010676319.1A CN202010676319A CN111848325B CN 111848325 B CN111848325 B CN 111848325B CN 202010676319 A CN202010676319 A CN 202010676319A CN 111848325 B CN111848325 B CN 111848325B
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separator
oil
mixer
phase
water
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CN111848325A (en
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杨建平
孙丽丽
白玫
余超
唐绮颖
李蓥菡
周换兰
何琨
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China Petroleum and Chemical Corp
Sinopec Shanghai Engineering Co Ltd
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Sinopec Shanghai Engineering Co Ltd
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    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C15/00—Cyclic hydrocarbons containing only six-membered aromatic rings as cyclic parts
    • C07C15/02—Monocyclic hydrocarbons
    • C07C15/085—Isopropylbenzene
    • 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
    • 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

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Abstract

The utility model relates to a method and a system for alkaline washing of cumene raw materials by a CHPPO device, which mainly solve the problems of imperfect flow and large equipment investment in the prior art. By adopting the method and the system, in a CHPPO device of 5-80 ten thousand tons/year, a mixing-gathering-mixing-hydrocyclone-separating alkaline washing process is adopted, and an oil phase, a water phase and a water phase in the discharging of a gathering device, a hydrocyclone and a separator are set, wherein the water phase is allowed to contain 2.0-9.0wt% of another water phase, the oil phase and the oil phase; the method is characterized in that 100-5000mg/kg of acid-containing cumene is subjected to alkaline washing treatment to obtain purified cumene with the organic acid content less than or equal to 50mg/kg, 41000-155000 kg of steel is saved, and investment is saved by 26.86-37.27%, so that the problems are well solved, and the method can be applied to PO production in CHPPO industrial devices.

Description

Method and system for alkaline washing of cumene raw material by CHPPO device
Technical Field
The utility model relates to the technical field of propylene oxide, in particular to a method and a system for removing organic acid impurities by alkaline washing of cumene raw materials of a CHPPO device by adopting a mixer, an accumulator and a hydrocyclone.
Background
The current industrial production technology of propylene oxide PO at home and abroad comprises the following steps: chlorohydrin process, direct oxidation process, indirect oxidation process, and the like. The main raw materials of the chlorohydrin method are chlorine and propylene, and the production process is divided into three parts: chlorohydrination, saponification and refining. The process has the advantages of simple technical flow, mature application, low requirement on raw material specification, good product selectivity, strong material corrosiveness, large amount of waste water and waste residue generated in the production process and high environmental protection pressure. The direct oxidation method is a novel process with simple flow, less byproducts and no pollution, and has the defects that the amount of the generated wastewater is relatively large, and an independent torch system is needed to solve the problem of oxygen-containing exhaust gas. The indirect oxidation method mainly comprises a PO co-production styrene SM process and a CHPPO process without a co-product. The former has high requirements on raw material specification and complex process, has large co-production product quantity and high requirements on large-scale production, and is suitable for construction in areas needing styrene. The latter has general requirements on raw material specification, simple process, high product yield, good stability and almost no byproducts, and is an energy-saving and environment-friendly green process. Considering the requirements of the planning development and the sustainable development of the petrochemical industry in China, the ratio selection of the technical scheme of the process can be as follows: the CHPPO process is one of the best process technologies for producing propylene oxide. The technological process adopts propylene as material and cumene hydroperoxide CHP as oxidant to epoxidize propylene to produce propylene oxide PO. The method mainly comprises the following steps: oxidizing cumene to generate CHP, and performing epoxidation reaction on the CHP and propylene to generate oxidation reaction products such as epoxypropane, dimethylbenzyl alcohol and the like; separating and refining the reaction product to obtain a high-quality PO product; and the dimethyl benzyl alcohol is subjected to hydrogenolysis to generate isopropylbenzene which is then oxidized into CHP for recycling. In the process of producing propylene oxide by a CHPPO method, in order to ensure that the reaction of oxidizing cumene to produce cumene hydroperoxide CHP can be more efficient and quicker, the organic acid impurities in the cumene raw material need to be removed to below 50 mg/kg.
The utility model 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 utility model patent application number of the prior art is CN201920293119.0 centrifugal sedimentation separator, which comprises a rotary separation device, an ingress pipe connected to one side of the rotary separation device, a clarified fluid delivery 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 a rotary separation tank, at least two conical cylinders arranged at intervals up and down in the rotary separation tank, a clarified fluid rising pipe connected to the bottom end of the rotary separation tank and jet pipes connected to 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 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 ends of the sedimentation separation tank, one end of the ingress pipe extends into the rotary separation tank and forms tapered conical nozzles, the sedimentation separation tank comprises a cylinder body and a cone body, and the bottom end of the cone body is connected with a discharge pipe. The centrifugal sedimentation separator has simple structure and higher separation effect.
The utility model patent application number in the prior art is CN201110445155.2, a method for recycling ethylene gas from tail gas and a water alkali washing tower thereof, wherein the tail gas from a buffer tank (1) enters the lower section through a gas inlet (14), enters the middle section through a bypass gas pipe (8) after exchange and absorption with water are completed, enters the upper section through a bypass gas pipe (9) after exchange and absorption with alkali liquor with the concentration of 1-3% are completed in the section, exchanges and absorbs 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 utility model patent application number in 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 removing organic acid impurities in the cumene raw material of a CHPPO device is not involved. The utility model patent application number is CN201920293119.0 centrifugal sedimentation separator, only discloses the operation function of a single device, and does not relate to the technical steps of connecting the whole process flow to remove the organic acid impurities in the cumene raw material of the CHPPO device by alkali elution. The utility model relates to a method for recovering ethylene gas from tail gas and a water-alkali washing tower thereof, and the method has the patent application number of CN201110445155.2, and only discloses a technical means for treating ethylene gas by adopting an alkali washing tower/water washing tower with high equipment engineering investment and high operation and running cost. Therefore, the prior art has the problems of imperfect technological process and large equipment engineering investment in the process of treating the cumene raw material by the CHPPO device.
Disclosure of Invention
In order to solve the problems in the prior art, the utility model provides a method and a system for alkaline washing of cumene raw materials by a CHPPO device, so that the process flow is further perfected, and the equipment engineering investment is reduced.
In order to achieve the above purpose, the present utility model adopts the following technical scheme:
the first aspect of the utility model provides a method for alkaline washing of cumene raw material in a CHPPO device, which comprises the following process flows in a commercial CHPPO industrial production device with nominal capacity of 5-80 ten thousand tons per year:
a) The method comprises the steps of dispersing acid-containing isopropylbenzene containing organic acid impurities in liquid drops in a first mixer, carrying out liquid-liquid contact, oil-water combination and full mixing on acid-containing isopropylbenzene, carrying out neutralization reaction on the organic acid impurities in the acid-containing isopropylbenzene, carrying out circulating alkali liquid after pressurization by a liquid pump of an aggregator, and carrying out liquid alkali neutralization reaction on the acid-containing isopropylbenzene and the circulating alkali liquid and the returned alkali liquid after pressurization by a water phase booster pump;
b) The mixed material flowing out of the first mixer enters an aggregation separator containing three layers of special materials, tiny oil drop particles are aggregated to form a continuous oil phase by utilizing the characteristics of oleophilic hydrophobic materials, and tiny water drop particles are aggregated to form a continuous water phase by utilizing the characteristics of oleophobic hydrophilic materials, so that the layered separation of oil and water is realized; the aggregator oil phase allows for a small amount of aqueous phase; the water phase of the collector does not allow oil phase to be contained, one part of the water phase of the collector enters the first mixer as a circulating alkali liquid after being pressurized by a liquid pump of the kettle of the collector, and the other part of the water phase of the collector is taken as a waste alkali liquid to be sent out of the tank;
c) The oil phase of the above-mentioned collector which has not completely removed the organic acid impurity and the oil phase of the separator which is pressurized by the oil phase booster pump are dispersed with the liquid drops in the second mixer, the liquid-liquid contact, the oil-water combination and the full mixing, the organic acid impurity which has not completely removed in the oil phase of the collector and the oil phase of the separator are neutralized and reacted with the liquid alkali in the fresh alkali liquid and the two-cycle alkali liquid;
d) The second mixed material flowing out of the second mixer after oil-water mixing enters a hydrocyclone, and oil phase and water phase with different densities are gathered and separated by utilizing centrifugal force generated in the hydrocyclone; the hydrocyclone oil phase flowing out of the hydrocyclone does not allow the aqueous phase, and is sent out of the boundary as purified isopropylbenzene;
e) The water phase of the cyclone liquid separator containing a small amount of oil phase, which flows out of the cyclone liquid separator, enters an oil-water separator, and after oil-water separation, the flowing out oil phase of the separator returns to the second mixer after being pressurized by an oil phase booster pump; the water phase of the separator flowing out of the oil-water separator is allowed to contain a small amount of oil phase, the oil phase is divided into two parts after being pressurized by the water phase booster pump, one part of the oil phase is used as return alkali liquor to return to the first mixer, and the other part of the oil phase is used as secondary alkali liquor to return to the second mixer.
Further, ethylbenzene in acid-containing cumene from outside the boundary 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 organic acid impurities is 100-5000mg/kg.
It is further preferred that ethylbenzene in acid-containing cumene from outside the boundary is not more than 0.10 wt.%, propylbenzene is not more than 0.05 wt.%, ding Ben 0.03.03 wt.%, and the organic acid impurity content is 200-2000mg/kg.
More preferably, the ethylbenzene in acid-containing cumene from outside the boundary is less than or equal to 0.01wt%, the propylbenzene is less than or equal to 0.01wt%, the Ding Ben 0.01.01 wt% and the organic acid impurity content is 500-1000mg/kg.
Further, the first mixer operates at a pressure of 0.57-1.17MPaA and an operating temperature of 25-85 ℃; the agglomerate separator operating pressure is 0.50-1.10MPaA, the operating temperature is 25-85 ℃, the agglomerate oil phase is allowed to contain 2.0-9.0wt% of aqueous phase; the second mixer operates at a pressure of 0.45-1.05MPaA and an operating temperature of 25-85 ℃; the operating pressure of the hydrocyclone is 0.38-0.98MPaA, the operating temperature is 25-85 ℃, and the aqueous phase of the hydrocyclone is allowed to contain 2.0-9.0wt% of oil phase; the oil-water separator is operated at a pressure of 0.35 to 0.95MPaA and at a temperature of 25 to 85 ℃, the separator water phase being allowed to contain 2.0 to 9.0wt% of the oil phase.
Further preferably, the first mixer is operated at a pressure of 0.67 to 1.07MPaA and at a temperature of 35 to 75 ℃; the agglomerate separator operating pressure is 0.60-1.00MPaA, the operating temperature is 35-75 ℃, the agglomerate oil phase is allowed to contain 3.0-8.0wt% aqueous phase; the second mixer operates at a pressure of 0.55-0.95MPaA and an operating temperature of 35-75deg.C; the operating pressure of the hydrocyclone is 0.48-0.88MPaA, the operating temperature is 35-75 ℃, and the aqueous phase of the hydrocyclone is allowed to contain 3.0-8.0wt% of oil phase; the oil-water separator is operated at a pressure of 0.45-0.85MPaA and at a temperature of 35-75deg.C, and the separator water phase is allowed to contain 3.0-8.0wt% oil phase.
More preferably, the first mixer is operated at a pressure of 0.77 to 0.97MPaA and an operating temperature of 45 to 65 ℃; the agglomerate separator operating pressure is 0.70-0.90MPaA, operating temperature is 45-65 ℃, the agglomerate oil phase is allowed to contain 4.0-7.0wt% aqueous phase; the second mixer operates at a pressure of 0.65-0.85MPaA and an operating temperature of 45-65deg.C; the operating pressure of the hydrocyclone is 0.58-0.78MPaA, the operating temperature is 45-65 ℃, and the aqueous phase of the hydrocyclone is allowed to contain 4.0-7.0wt% of oil phase; the oil-water separator is operated at a pressure of 0.55-0.75MPaA and at a temperature of 45-65deg.C, and the separator water phase is allowed to contain 4.0-7.0wt% oil phase.
The second aspect of the utility model provides a system for alkaline washing of cumene raw material by a CHPPO device based on the method, which comprises the following steps:
a first mixer;
the aggregation separator is connected with the first mixer through a pipeline;
the collector kettle liquid pump is connected with the collector separator and the first mixer through a pipeline;
the second mixer is connected with the gathering separator through a pipeline;
the hydrocyclone is connected with the second mixer through a pipeline;
the oil-water separator is connected with the hydrocyclone through a pipeline;
the oil phase booster pump is connected with the oil-water separator and the second mixer through pipelines;
and the water phase booster pump is connected with the oil-water separator, the first mixer and the second mixer through pipelines.
Further, the three layers of special materials in the aggregation separator sequentially comprise an oleophilic hydrophobic material, an oleophobic hydrophilic material and an oleophilic hydrophobic material, wherein the oleophilic hydrophobic material is one of glass fiber, PET hollow fiber, PP hollow fiber and oil-absorbing cotton fiber; the oleophobic hydrophilic material is one material of modified fiber, composite fiber, tiO2 nanofiber and absorbent cotton fiber.
Compared with the prior art, the utility model has the following technical effects:
the utility model relates to a method and a system for alkaline washing cumene raw materials of a CHPPO device, which adopts the alkaline washing process flow of a first mixer-gathering separator-second mixer-hydrocyclone-oil-water separator to replace the process flow of an alkaline washing tower in the prior art, and sets the oil phase, the water phase and the water phase in the discharging of the gathering separator, the hydrocyclone and the oil-water separator to allow the content of the other water phase, the oil phase and the oil phase to be 2.0-9.0wt% for the commercial CHPPO industrial production device with the nominal capacity of 5-80 ten thousand tons per year; the cumene raw material from the outside of the world containing 100-5000mg/kg of organic acid impurities is subjected to alkali washing deacidification treatment to obtain purified cumene with the organic acid impurity content less than or equal to 50mg/kg, the weight of equipment steel can be saved by 41000-155000 kg, the equipment engineering investment is saved by 26.86-37.27%, and a better technical effect is achieved.
Drawings
FIG. 1 is a schematic process flow diagram of a process for caustic washing cumene feed;
wherein, the A-first mixer, the B-gathering separator, the C-gathering still liquid pump, the D-second mixer, the E-oil phase booster pump, the F-hydrocyclone, the G-oil-water separator, the H-water phase booster pump, the 11-acid-containing cumene, the 12-one mixed material, the 13-gathering still oil phase, the 14-two mixed material, the 15-separator oil phase, the 16-purified cumene, the 21-waste lye, the 22-one circulation lye, the 23-return lye, the 24-gathering still water phase, the 25-two circulation lye, the 26-hydrocyclone water phase, the 27-separator water phase and the 28-fresh lye;
the process flow of the utility model is described as follows:
the acid-containing cumene 11 from the impurities of the organic acid outside the boundary is combined with the returned alkali liquor 23 after being pressurized by the water phase booster pump H and enters the first mixer A, the first mixed liquor 22 after being pressurized by the collector kettle liquid pump C also enters the first mixer A, the effluent mixed liquor 12 enters the collector separator B after being mixed with oil and water, the effluent collector oil phase 13 after being collected and separated is combined with the fresh alkali liquor 28 from the outside the boundary and enters the second mixer D, the second mixed liquor 25 after being pressurized by the water phase booster pump H also enters the second mixer D, the separator oil phase 15 after being pressurized by the oil phase booster pump E also enters the second mixer D, the effluent second mixed liquor 14 after being mixed with oil and water enters the cyclone separator F, and the effluent cyclone oil phase after being separated by cyclone is taken as purified cumene 16 to be sent out of the boundary. Part of the aqueous phase 24 of the collector flowing out of the collector separator B is pressurized by the collector tank liquid pump C and then enters the first mixer A as a circulating alkali liquor 22, and the other part of the aqueous phase of the collector is sent out of the tank as a waste alkali liquor 21. The cyclone water phase 26 flowing out of the cyclone separator F enters an oil-water separator G, after oil-water separation, the flowing-out separator oil phase 15 is pressurized by an oil phase booster pump E and enters a second mixer D, a part of the water phase 27 flowing out of the oil-water separator G, after being pressurized by an aqueous phase booster pump H, enters a first mixer A as return alkali liquor 23, and the other part of the water phase 27 enters the second mixer D as secondary alkali liquor 25.
Detailed Description
The utility model provides a method and a system for alkaline washing of cumene raw materials by a CHPPO device. The present utility model will be described in detail and in detail by way of the following examples, which are not intended to limit the scope of the utility model, for better understanding of the utility model.
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 single weight of equipment is 110000 kg. 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 alkaline washing of cumene raw material by 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 is combined with the returned alkali liquor 23 after being pressurized by the water phase booster pump H and enters the first mixer A, the first mixed liquor 22 after being pressurized by the collector kettle liquid pump C also enters the first mixer A, the effluent mixed liquor 12 enters the collector separator B after being mixed with oil and water, the effluent collector oil phase 13 after being collected and separated is combined with the fresh alkali liquor 28 from the outside the boundary and enters the second mixer D, the second mixed liquor 25 after being pressurized by the water phase booster pump H also enters the second mixer D, the separator oil phase 15 after being pressurized by the oil phase booster pump E also enters the second mixer D, the effluent second mixed liquor 14 after being mixed with oil and water enters the cyclone separator F, and the effluent cyclone oil phase after being separated by cyclone is taken as purified cumene 16 to be sent out of the boundary. Part of the aqueous phase 24 of the collector flowing out of the collector is pressurized by the collector tank liquid pump C and then enters the first mixer A as a circulating alkali liquor 22, and the other part of the aqueous phase of the collector is sent out of the tank as a waste alkali liquor 21. The cyclone water phase 26 flowing out of the cyclone liquid separator enters an oil-water separator G, after oil-water separation, the flowing-out separator oil phase 15 enters a second mixer D after being pressurized by an oil phase booster pump E, and part of the water phase 27 flowing out of the oil-water separator enters the first mixer A as return alkali liquor 23 after being pressurized by an aqueous phase booster pump H, and the other part of the water phase enters the second mixer D as secondary alkali liquor 25.
In the commercial industrial production device with the nominal capacity of 5 ten thousand tons/year, the aggregate separator device parameter in the main device is phi 3000×11500mm, the single weight of the device is 37000 kg, the hydrocyclone device parameter is phi 2000×6300mm, the single weight of the device is 14000 kg, the oil-water separator device parameter is phi 2400×7500mm, the single weight of the device is 18000 kg, and the total weight of 3 main devices is 69000 kg. The content of organic acid impurity from the acid cumene outside the boundary is 120mg/kg, and after the alkaline washing treatment of the first mixer-aggregation separator-second mixer-hydrocyclone-oil-water separator in this example, 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 1, the method can save 41000 kg of equipment steel, save 37.27% of equipment engineering investment and obtain better technical effect.
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 main equipment alkaline washing towers are phi 4400 multiplied by 40000mm, and the equipment weight is 163000 kilograms. 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 to example 1, the nominal capacity of the CHPPO apparatus was changed to a commercial industrial production apparatus of 10 ten thousand tons/year, the aggregate separator device parameter in the main device was Φ4600×12200mm, the device weight was 59000 kg, the hydrocyclone device parameter was Φ2800×6600mm, the device weight was 20000 kg, the oil-water separator device parameter was Φ3200×8000mm, the device weight was 27000 kg, and the total weight of 3 main devices was 106000 kg. After the alkaline washing treatment of the first mixer-aggregation separator-second mixer-hydrocyclone-oil-water separator of this example, purified cumene with an organic acid impurity content of 50mg/kg or less was obtained from the acid cumene outside the boundary, and other process data are shown in Table 2. Compared with the method of the comparative example 2, 57000 kg of equipment steel can be saved, 34.97% of equipment engineering investment is saved, and a better technical effect is achieved.
[ 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 main equipment alkaline washing towers are phi 6000 multiplied by 44000mm, and the single weight of equipment is 254000 kg. 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, the nominal capacity of the CHPPO apparatus was changed to a commercial industrial production apparatus of 20 ten thousand tons/year, the aggregate separator device parameter in the main device was Φ6800×13400mm, the device weight was 100000 kg, the hydrocyclone device parameter was Φ4000×7300mm, the device weight was 32000 kg, the oil-water separator device parameter was Φ4600×8800mm, the device weight was 43000 kg, and the total weight of 3 main devices was 175000 kg. After alkali washing treatment of the first mixer-aggregation separator-second mixer-hydrocyclone-oil-water separator of this example, purified cumene with an organic acid impurity content of 50mg/kg or less was obtained from the acid cumene outside the boundary, and other process data are shown in Table 2. Compared with the method of the comparative example 3, the weight of the equipment steel is 79000 kg, the equipment engineering investment is saved by 31.10%, and a better technical effect is achieved.
[ 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 equipment weight is 346000 kg. 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 ]
Similarly to example 1, the commercial industrial production facility with only a CHPPO device having a nominal capacity of 40 ten thousand tons/year was changed to a main device having an aggregate separator device parameter of Φ10000×14200mm, a device weight of 140000 kg, a hydrocyclone device parameter of Φ5800×7800mm, a device weight of 43000 kg, an oil-water separator device parameter of Φ6400×9300mm, a device weight of 57000 kg, and a total of 3 main devices of 240000 kg. After the alkaline washing treatment of the first mixer-aggregation separator-second mixer-hydrocyclone-oil-water separator of the present example, the purified cumene with the organic acid impurity content of 50mg/kg or less was obtained from the acid cumene outside the boundary, and other process data are shown in Table 2. Compared with the method of the comparative example 4, the method can save 106000 kg of equipment steel, save 30.64% of equipment engineering investment and obtain 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 equipment weight is 423000 kg. 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 to example 1, the commercial industrial production facility with only a CHPPO device having a nominal capacity of 40 ten thousand tons/year was changed to a commercial industrial production facility with a main equipment having an aggregate separator equipment parameter of Φ10000×14000mm, an equipment weight of 169000 kg, a hydrocyclone equipment parameter of Φ5800×7600mm, an equipment weight of 51000 kg, an oil-water separator equipment parameter of Φ6400×9100mm, an equipment weight of 69000 kg, and a total of 3 main equipment weights of 289000 kg. After the alkaline washing treatment of the first mixer-aggregation separator-second mixer-hydrocyclone-oil-water separator of the present example, purified cumene with the organic acid impurity content of 50mg/kg or less was obtained from the acid cumene outside the boundary, and other process data are shown in Table 2. Compared with the method of the comparative example 5, the weight of equipment steel is 134000 kg, the equipment engineering investment is saved by 31.68%, and a better technical effect is achieved.
[ 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 equipment weight is 577000 kg. 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 ]
Similarly to example 1, the nominal capacity of the CHPPO unit was changed to 80 ten thousand tons/year commercial industrial production unit, the aggregate separator device parameter in the main device was Φ15200×15400mm, the device weight per unit was 252000 kg, the hydrocyclone device parameter was Φ8000×8400mm, the device weight per unit was 73000 kg, the oil-water separator device parameter was Φ9000×10000mm, the device weight per unit was 97000 kg, and the total weight of 3 main devices was 422000 kg. After the alkaline washing treatment of the first mixer-aggregation separator-second mixer-hydrocyclone-oil-water separator of the present example, purified cumene with an organic acid impurity content of 50mg/kg or less was obtained from the acid cumene outside the boundary, and other process data are shown in Table 2. Compared with the method of the comparative example 6, 155000 kg of equipment steel can be saved, 26.86% of equipment engineering investment can be saved, and a better technical effect can be achieved.
TABLE 1 prior art caustic tower Process data List
Figure BDA0002584184690000101
TABLE 2 list of major plant Process data for the utility model
Figure BDA0002584184690000111
Figure BDA0002584184690000121
The above description of the specific embodiments of the present utility model has been given by way of example only, and the present utility model 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 utility model are intended to be within the scope of the present utility model. Accordingly, equivalent changes and modifications are intended to be included within the scope of the present utility model without departing from the spirit and scope thereof.

Claims (7)

1. A method for alkaline washing of cumene raw material by a CHPPO device, which is characterized by comprising the following steps: in a commercial CHPPO industrial production device with a nominal capacity of 5-80 ten thousand tons/year, the method comprises the following process flows:
a) The method comprises the steps that acid-containing isopropyl benzene (11) containing organic acid impurities is in liquid drop dispersion, liquid-liquid contact, oil-water combination and full mixing in a first mixer (A) with primary alkali circulating liquid (22) pressurized by an aggregator kettle liquid pump (C) and return alkali liquid (23) pressurized by an aqueous phase booster pump (H), and the organic acid impurities in the acid-containing isopropyl benzene (11) are subjected to neutralization reaction with the primary alkali circulating liquid (22) and the alkali liquid in the return alkali liquid (23) to be removed;
b) A mixed material (12) flowing out of the first mixer (A) enters an aggregation separator (B) containing three layers of special materials, tiny oil drop particles are aggregated to form a continuous oil phase by utilizing the characteristics of oleophilic and hydrophobic materials, and tiny water drop particles are aggregated to form a continuous water phase by utilizing the characteristics of oleophobic and hydrophilic materials, so that oil-water layering separation is realized; the aggregator oil phase (13) is allowed to contain a small amount of aqueous phase; the water phase of the collector does not allow oil phase, one part of the water phase (24) of the collector is pressurized by a liquid pump (C) of the collector and then enters the first mixer (A) as a circulating alkali liquid (22), and the other part of the water phase (24) of the collector is sent out of the tank as a waste alkali liquid (21);
c) The oil phase (13) of the collector which is not completely removed of the organic acid impurities and the oil phase (15) of the separator which is pressurized by the oil phase booster pump (E) are subjected to neutralization reaction with fresh lye (28) from outside and secondary lye (25) which is pressurized by the water phase booster pump (H) in a second mixer (D) to remove the organic acid impurities which are not completely removed in the oil phase (13) of the collector and the oil phase (15) of the separator, and the fresh lye (28) and the liquid caustic in the secondary lye (25);
d) The second mixed material (14) flowing out of the second mixer (D) after oil-water mixing enters a hydrocyclone (F), and oil phase and water phase with different densities are gathered and separated by utilizing centrifugal force generated in the hydrocyclone (F) hydrocyclone process; the hydrocyclone oil phase flowing out of the hydrocyclone (F) does not allow an aqueous phase, which is sent out of the tank as purified cumene (16);
e) A hydrocyclone water phase (26) containing a small amount of oil phase and flowing out of the hydrocyclone (F) enters an oil-water separator (G), and after oil-water separation, the flowing-out separator oil phase (15) returns to the second mixer (D) after being pressurized by an oil phase booster pump (E); the separator water phase (27) flowing out of the oil-water separator (G) is allowed to contain a small amount of oil phase, and is divided into two parts after being pressurized by a water phase booster pump (H), one part of the oil phase is used as the return alkali liquor (23) to return to the first mixer (A), and the other part of the oil phase is used as the secondary alkali liquor (25) to return to the second mixer (D);
the system for alkaline washing of the cumene raw material by the CHPPO device adopted by the method comprises the following steps:
-said first mixer (a);
the aggregation separator (B) is connected with the first mixer (A) through a pipeline;
the collector tank liquid pump (C) is connected with the collector separator (B) and the first mixer (A) through a pipeline;
the second mixer (D) is connected to the aggregation separator (B) by a pipe;
the hydrocyclone (F) is connected with the second mixer (D) through a pipeline;
the oil-water separator (G) is connected with the hydrocyclone (F) through a pipeline;
the oil phase booster pump (E) is connected with the oil-water separator (G) and the second mixer (D) through pipelines;
the water phase booster pump (H) is connected with the oil-water separator (G), the first mixer (A) and the second mixer (D) through pipelines;
the three-layer special material in the aggregation separator (B) sequentially comprises an oleophilic and hydrophobic material, an oleophobic and hydrophilic material and an oleophilic and hydrophobic material, wherein the oleophilic and hydrophobic material is one material of glass fiber, PET hollow fiber, PP hollow fiber and oil-absorbing cotton fiber; the oleophobic hydrophilic material is one material of modified fiber, composite fiber, tiO2 nanofiber and absorbent cotton fiber.
2. The method for alkaline washing of cumene raw material of a CHPPO device according to claim 1, wherein ethylbenzene in the acid-containing cumene (11) from outside the boundary is less than or equal to 0.60 and wt%, cumene is less than or equal to 0.30 and wt%, ding Ben and 0.10 and wt%, and the organic acid impurity content is 100-5000mg/kg.
3. The method for alkaline washing of cumene raw material of a CHPPO device according to claim 2, wherein ethylbenzene in the acid-containing cumene (11) from outside the boundary is less than or equal to 0.10 and wt%, cumene is less than or equal to 0.05 and wt%, ding Ben and 0.03 and wt%, and the organic acid impurity content is 200-2000mg/kg.
4. A process for alkaline washing of cumene feed to a CHPPO plant as claimed in claim 3, characterized in that ethylbenzene in the acid-containing cumene (11) coming from outside the boundary is less than or equal to 0.01 and wt%, cumene is less than or equal to 0.01 and wt%, ding Ben and wt% and organic acid impurity content is 500-1000mg/kg.
5. The process for alkaline washing of cumene feed to a CHPPO plant according to claim 1, characterized in that the first mixer (a) is operated at a pressure of 0.57-1.17mpa and at an operating temperature of 25-85 ℃; said agglomeration separator (B) operating at a pressure of 0.50-1.10mpa and an operating temperature of 25-85 ℃, said agglomeration separator oil phase (13) allowing to contain 2.0-9.0wt% of an aqueous phase; the second mixer (D) is operated at a pressure of 0.45-1.05MPaA and at a temperature of 25-85 ℃; the operating pressure of the hydrocyclone (F) is 0.38-0.98MPaA, the operating temperature is 25-85 ℃, and the hydrocyclone water phase (26) is allowed to contain 2.0-9.0wt% oil phase; the oil-water separator (G) is operated at a pressure of 0.35-0.95MPaA and at a temperature of 25-85 ℃, and the separator water phase (27) is allowed to contain 2.0-9.0wt% oil phase.
6. The process for alkaline washing of cumene feed to a CHPPO plant as claimed in claim 5, characterized in that the first mixer (a) is operated at a pressure of 0.67-1.07mpa and at a temperature of 35-75 ℃; said agglomeration separator (B) operating at a pressure of 0.60-1.00MPaA and an operating temperature of 35-75deg.C, said agglomeration separator oil phase (13) allowing to contain 3.0-8.0wt% of an aqueous phase; the second mixer (D) has an operating pressure of 0.55-0.95MPaA and an operating temperature of 35-75 ℃; the operating pressure of the hydrocyclone (F) is 0.48-0.88MPaA, the operating temperature is 35-75 ℃, and the hydrocyclone water phase (26) is allowed to contain 3.0-8.0wt% oil phase; the oil-water separator (G) is operated at a pressure of 0.45-0.85MPaA and at a temperature of 35-75deg.C, and the separator water phase (27) is allowed to contain 3.0-8.0wt% oil phase.
7. The process for alkaline washing of cumene feed to a CHPPO plant as claimed in claim 6, characterized in that the first mixer (a) is operated at a pressure of 0.77-0.97mpa and at a temperature of 45-65 ℃; said agglomeration separator (B) operating at a pressure of 0.70-0.90mpa and an operating temperature of 45-65 ℃ and said agglomeration separator oil phase (13) allowed to contain 4.0-7.0wt% aqueous phase; the second mixer (D) has an operating pressure of 0.65-0.85MPaA and an operating temperature of 45-65 ℃; the operating pressure of the hydrocyclone (F) is 0.58-0.78MPaA, the operating temperature is 45-65 ℃, and the hydrocyclone water phase (26) is allowed to contain 4.0-7.0wt% oil phase; the oil-water separator (G) is operated at a pressure of 0.55-0.75MPaA and at a temperature of 45-65 ℃, and the aqueous separator phase (27) is allowed to contain 4.0-7.0wt% of the oil phase.
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