CN111848325A - Method and system for washing cumene raw material with alkali by using CHPPO (chlorinated Polypropylene oxide) device - Google Patents
Method and system for washing cumene raw material with alkali by using CHPPO (chlorinated Polypropylene oxide) device Download PDFInfo
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- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
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- 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
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Abstract
The invention relates to a method and a system for washing a cumene raw material by an alkali in a CHPPO device, which mainly solve the problems of incomplete 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, an alkali washing process of 'mixing-aggregating-mixing-hydrocyclone-separating' is adopted, and the oil phase, the water phase and the water phase in the discharge of a concentrator, a hydrocyclone and a separator are set to be allowed to contain 2.0-9.0 wt% of another water phase, an oil phase and an oil phase; the 100-containing acid cumene of 5000mg/kg is subjected to alkali washing treatment to obtain purified cumene of which the organic acid is less than or equal to 50mg/kg, 41000-155000 kg of steel is saved, the investment is saved by 26.86-37.27%, the problems are better solved, and the method can be applied to PO production by CHPPO industrial devices.
Description
Technical Field
The invention relates to the technical field of propylene oxide, in particular to a method and a system for removing organic acid impurities by adopting a mixer, a collector and a cyclone to combine a cumene raw material of an alkali washing CHPPO device.
Background
The current industrialized production technology of propylene oxide PO at home and abroad comprises the following steps: chlorohydrin method, direct oxidation method, indirect oxidation method and other typical process technologies. 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 process, mature application, low requirements on raw material specifications, good product selectivity, strong material corrosivity, large amount of waste water and waste residues generated in the production process, and high environmental protection pressure. The direct oxidation process is a new process with simple flow, less by-products and green and pollution-free, and has disadvantages in that the amount of waste water produced is relatively large and a separate flare system is required to solve the problem of oxygen-containing exhaust gas. The indirect oxidation method mainly comprises a PO coproduction styrene SM process and a CHPPO process without a coproduction product. The former has high requirements on raw material specifications, complex process, large quantity of co-produced products and higher requirements on large-scale production, and is suitable for construction in areas needing styrene. The latter has general requirements on raw material specifications, simple process, high product yield, good stability and almost no by-product, and is an energy-saving and environment-friendly green process. In consideration of the requirements of the petrochemical industry planning development and the sustainable development in China, the following technical schemes are selected: the CHPPO process is one of the best process technologies for producing propylene oxide. The technical route takes propylene as a raw material and cumene hydroperoxide CHP as an oxidant to epoxidize the propylene to generate propylene oxide PO. The method mainly comprises the following steps: oxidizing cumene to generate CHP, and carrying out epoxidation reaction on the CHP and propylene to generate oxidation reaction products such as propylene oxide, dimethyl benzyl alcohol ring and the like; separating and refining the reaction product to produce a high-quality PO product; the cumene generated by the hydrogenolysis of dimethyl benzyl alcohol is reoxidized to be CHP for recycling. In the process of producing propylene oxide by CHPPO method, in order to ensure that the reaction of oxidizing cumene to cumene hydroperoxide CHP can be more efficient and rapid, organic acid impurities in the cumene raw material need to be removed to be below 50 mg/kg.
The invention in the prior art has patent application number CN201910850055.4 and relates to a method for preparing cumene hydroperoxide by cumene oxidation, which comprises the following steps: cumene hydroperoxide is produced by oxidation of cumene in the presence of alpha-methylstyrene dimer. Preferably, the process is also carried out in the presence of a by-product inhibitor. When the reaction liquid contains a certain amount of alpha-methylstyrene dimer, the conversion rate of the cumene is improved, and after the alpha-methylstyrene dimer and the byproduct inhibitor are added simultaneously, the conversion rate of the cumene can be increased and the selectivity of the methyl phenyl ketone can be effectively reduced.
The utility model with the patent application number of CN201920293119.0 centrifugal sedimentation separator in the prior art comprises a rotary separation device, an ingress pipe connected to one side of the rotary separation device, a clarified fluid eduction 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 in the rotary separation tank at intervals up and down, a clarified fluid ascension pipe connected to the bottom end of the rotary separation tank and jet pipes connected to both sides of the rotary separation tank, the conical cylinders extend in a tapered shape from up to down along the inner wall of the rotary separation tank, the top ends of the two jet pipes correspond to both sides of the conical cylinder arranged at the uppermost layer in the rotary separation tank, the bottom end is connected with the top end of the sedimentation separation tank, one end of the ingress pipe extends into the rotary separation tank and forms a tapered conical spout, the sedimentation separation tank comprises a cylinder body and a conical body, the bottom end of the conical body is connected with a discharge pipe. The centrifugal sedimentation separator has a simple structure and a higher separation effect.
The invention patent application number in the prior art is CN201110445155.2 a method for recovering ethylene gas from tail gas and a water alkaline washing tower thereof, and discloses a method for recovering ethylene gas from tail gas, tail gas from a buffer tank (1) enters a lower section from a gas inlet (14), enters a middle section through a bypass gas pipe (8) after completing exchange absorption with water, enters an upper section through a bypass gas pipe (9) after completing exchange absorption with alkali liquor with the concentration of 1-3% in the middle section, exchanges absorption with water again, and is sent to a gas cabinet (7) from a gas outlet (15) after purification; water from the water circulation tank (3) firstly enters the upper section from a water inlet (16), enters the lower section through a bypass water pipe (10) after completing exchange absorption, and returns to the water circulation tank (3) from a water outlet (17) after completing exchange absorption; alkali liquor with the concentration of 1-3% from the alkali liquor circulating tank (5) enters the middle section from an alkali liquor inlet (18), and returns to the alkali liquor circulating tank (5) from an alkali liquor outlet (19) after exchange absorption is completed; the method can improve the content of the ethylene gas from 89.5 percent to 96.43 percent, and reduce the content of VAC from 9.49 percent to 2.57 percent.
The invention in the prior art is a method for preparing cumene hydroperoxide by oxidizing cumene, which has the patent application number of CN201910850055.4, only discloses a technical scheme for preparing the cumene hydroperoxide, and does not relate to a technical method for removing organic acid impurities in the cumene raw material of a CHPPO device. The utility model discloses a patent application number is CN201920293119.0 centrifugal sedimentation separator, only discloses the operational function of single unit equipment, does not relate to the technical step who connects whole process flow with alkali wash desorption CHPPO device isopropyl benzene raw materials in organic acid impurity. The invention discloses a method for recovering ethylene gas from tail gas and a water caustic wash tower thereof with the patent application number of CN201110445155.2, and only discloses a technical means for treating the ethylene gas by adopting a caustic wash tower/water wash tower with large equipment engineering investment and high operation and running cost. Therefore, in the prior art, the problems of incomplete process flow and large equipment engineering investment exist 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 invention provides a method and a system for washing a cumene raw material by an alkali in a CHPPO device, so that the process flow is further improved, and the equipment engineering investment is reduced.
In order to achieve the purpose, the invention adopts the following technical scheme:
the invention provides a method for alkaline washing of a cumene raw material by a CHPPO device, which comprises the following process flows in a large-scale commercial CHPPO industrial production device with nominal capacity of 5-80 ten thousand tons per year:
a) acid-containing cumene containing organic acid impurities, circulating alkali liquor pressurized by a collector kettle liquor pump and return alkali liquor pressurized by a water phase booster pump are subjected to liquid drop dispersion, liquid-liquid contact, oil-water combination and full mixing in a first mixer, and the organic acid impurities in the acid-containing cumene, the circulating alkali liquor and the liquid alkali in the return alkali liquor are subjected to neutralization reaction and are removed;
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 oleophylic 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 oil-water layered separation is realized; the collector oil phase is allowed to contain a small amount of water phase; the water phase of the collector does not allow oil-containing phase, one part of the water phase of the collector is pressurized by a collector kettle liquid pump and then enters the first mixer as circulating alkali liquid, and the other part of the water phase of the collector is sent out as waste alkali liquid;
c) The oil phase of the collector and the oil phase of the separator after being pressurized by the oil phase booster pump, which are not completely removed with organic acid impurities, are dispersed, contacted, combined and fully mixed with liquid drops of fresh alkali liquor from outside and secondary circulating alkali liquor after being pressurized by the water phase booster pump in a second mixer, and the organic acid impurities which are not completely removed in the oil phase of the collector and the oil phase of the separator are neutralized and removed with liquid alkali in the fresh alkali liquor and the secondary circulating alkali liquor;
d) the second mixed material which flows out after the oil and the water are mixed in the second mixer enters a hydrocyclone separator, and the oil phase and the water phase with different densities are gathered and separated by using the centrifugal force generated in the hydrocyclone separator liquid rotating process; the hydrocyclone oil phase which flows out of the hydrocyclone does not allow an aqueous phase, which is sent out as purified cumene;
e) the water phase of the hydrocyclone containing a small amount of oil phase flowing out of the hydrocyclone enters an oil-water separator, and after oil-water separation, the oil phase flowing out of the separator is pressurized by an oil phase booster pump and then returns to the second mixer; 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 a water phase booster pump, one part of the oil phase is returned to the first mixer as return alkali liquor, and the other part of the oil phase is returned to the second mixer as secondary circulation alkali liquor.
Furthermore, the ethylbenzene in the acid-containing cumene from outside is less than or equal to 0.60 wt%, the propylbenzene is less than or equal to 0.30 wt%, the butylbenzene is less than or equal to 0.10 wt%, and the organic acid impurity content is 100-5000 mg/kg.
Further preferably, the ethylbenzene in the acid-containing cumene from the outside is less than or equal to 0.10 wt%, the propylbenzene is less than or equal to 0.05 wt%, the butylbenzene is less than or equal to 0.03 wt%, and the organic acid impurity content is 200-2000 mg/kg.
More preferably, the ethylbenzene in the acid-containing cumene from the outside is less than or equal to 0.01 wt%, the propylbenzene is less than or equal to 0.01 wt%, the butylbenzene is less than or equal to 0.01 wt%, and the organic acid impurity content is 500-1000 mg/kg.
Further, the first mixer is operated at a pressure of 0.57-1.17MPaA and at a temperature of 25-85 ℃; the operation pressure of the aggregation separator is 0.50-1.10MPaA, the operation temperature is 25-85 ℃, and the oil phase of the aggregation separator is allowed to contain 2.0-9.0 wt% of water phase; the operating pressure of the second mixer is 0.45-1.05MPaA, and the operating temperature is 25-85 ℃; the operating pressure of the hydrocyclone is 0.38-0.98MPaA, the operating temperature is 25-85 ℃, and the water phase of the hydrocyclone is allowed to contain 2.0-9.0 wt% of oil phase; the oil-water separator is operated at a pressure of 0.35-0.95MPaA and at a temperature of 25-85 deg.C, and the water phase of the separator is allowed to contain 2.0-9.0 wt% 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 operation pressure of the aggregation separator is 0.60-1.00MPaA, the operation temperature is 35-75 ℃, and the oil phase of the aggregation separator is allowed to contain 3.0-8.0 wt% of water phase; the second mixer is operated at a pressure of 0.55-0.95MPaA and at a temperature of 35-75 ℃; the operating pressure of the hydrocyclone is 0.48-0.88MPaA, the operating temperature is 35-75 ℃, and the water phase of the hydrocyclone is allowed to contain 3.0-8.0 wt% of oil phase; the oil-water separator is operated at a pressure of 0.45-0.85MPaA and at a temperature of 35-75 deg.C, and the water phase of the separator is allowed to contain 3.0-8.0 wt% of oil phase.
More preferably, the first mixer is operated at a pressure of 0.77-0.97MPaA and at a temperature of 45-65 ℃; the operation pressure of the aggregation separator is 0.70-0.90MPaA, the operation temperature is 45-65 ℃, and the oil phase of the aggregation separator is allowed to contain 4.0-7.0 wt% of water phase; the operating pressure of the second mixer is 0.65-0.85MPaA, and the operating temperature is 45-65 ℃; the operating pressure of the hydrocyclone is 0.58-0.78MPaA, the operating temperature is 45-65 ℃, and the water phase of the hydrocyclone is allowed to contain 4.0-7.0 wt% of oil phase; the oil-water separator is operated at a pressure of 0.55-0.75MPaA and a temperature of 45-65 deg.C, and the water phase of the separator is allowed to contain 4.0-7.0 wt% of oil phase.
The second aspect of the invention provides a system for alkali washing of a raw material of isopropyl benzene in 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 collection separator and the first mixer through pipelines;
a second mixer connected to the aggregation separator through a pipe;
the hydrocyclone separator is connected with the second mixer through a pipeline;
the oil-water separator is connected with the hydrocyclone separator 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.
Furthermore, the three layers of special materials in the gathering separator sequentially consist of an oleophylic hydrophobic material, an oleophobic hydrophilic material and an oleophylic hydrophobic material, wherein the oleophylic hydrophobic material is one of glass fiber, PET hollow fiber, PP hollow fiber and oil absorbent cotton fiber; the oleophobic hydrophilic material is one of modified fiber, composite fiber, TiO2 nanofiber and absorbent cotton fiber.
By adopting the technical scheme, compared with the prior art, the invention has the following technical effects:
the invention relates to a method and a system for washing cumene raw materials with alkali by a CHPPO device, wherein for a large-scale commercial CHPPO industrial production device with nominal capacity of 5-80 ten thousand tons/year, the alkali washing process flow of a first mixer, an aggregation separator, a second mixer, a hydrocyclone separator and an oil-water separator is adopted to replace the process flow of an alkali washing tower in the prior art, and an oil phase, a water phase and a water phase in the discharge materials of the aggregation separator, the hydrocyclone separator and the oil-water separator are set to allow another water phase, an oil phase and an oil phase to contain 2.0-9.0 wt%; the cumene raw material containing 5000mg/kg of organic acid impurity from outside is subjected to alkali washing deacidification treatment to obtain the 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 can be saved by 26.86-37.27%, and better technical effects are obtained.
Drawings
FIG. 1 is a schematic diagram of a process flow of a process for caustic washing a cumene feedstock;
wherein, A-a first mixer, B-a gathering separator, C-a gathering kettle liquid pump, D-a second mixer, E-an oil phase booster pump, F-a hydrocyclone separator, G-an oil-water separator, H-a water phase booster pump, 11-acid-containing cumene, 12-a mixed material, 13-a gathering oil phase, 14-a mixed material, 15-a separator oil phase, 16-purified cumene, 21-waste lye, 22-a circulating lye, 23-a return lye, 24-a gathering water phase, 25-a circulating lye, 26-a hydrocyclone water phase, 27-a separator water phase and 28-a fresh lye;
the process flow of the invention is described as follows:
acid-containing cumene 11 containing organic acid impurities from the outside and return alkali liquor 23 pressurized by a water phase booster pump H are combined and enter a first mixer A, primary circulating alkali liquor 22 pressurized by a collector kettle liquid pump C also enters the first mixer A, an outflow primary mixed material 12 enters an aggregation separator B after oil-water mixing, an outflow collector oil phase 13 and fresh alkali liquor 28 from the outside are combined and enter a second mixer D after aggregation separation, a secondary circulating alkali liquor 25 pressurized by the water phase booster pump H also enters the second mixer D, a separator oil phase 15 pressurized by an oil phase booster pump E also enters the second mixer D, an outflow secondary mixed material 14 enters a hydrocyclone F after oil-water mixing, and an outflow hydrocyclone oil phase is taken as purified cumene 16 to be sent out of the outside after hydrocyclone separation. A part of the collector aqueous phase 24 flowing out of the collector-separator B is pressurized by the collector still pump C and then enters the first mixer A as a circulating lye 22, and the other part of the collector aqueous phase is sent out as a waste lye 21. And the hydrocyclone water phase 26 flowing out of the hydrocyclone F enters an oil-water separator G, after oil-water separation, the outflow separator oil phase 15 is pressurized by an oil phase booster pump E and then enters a second mixer D, one part of the separator water phase 27 flowing out of the oil-water separator G is pressurized by a water phase booster pump H and then enters a first mixer A as a return alkali liquor 23, and the other part of the separator water phase 27 enters the second mixer D as a secondary circulating alkali liquor 25.
Detailed Description
The invention provides a method and a system for washing a cumene raw material by an alkali in a CHPPO device. The present invention will be described in detail and specifically with reference to the following examples to facilitate better understanding of the present invention, but the following examples do not limit the scope of the present invention.
Comparative example 1
In the prior art, a conventional alkaline washing tower process flow is adopted to carry out alkaline washing treatment on an acid-containing cumene raw material, a CHPPO device is a commercial industrial production device with nominal capacity of 5 ten thousand tons/year, the equipment parameters of an alkaline washing tower of main equipment are phi 3000 multiplied by 38000mm, and the unit weight of the equipment is 110000 kilograms. The organic acid impurity content in the acid-containing cumene from the outside is 200-1000mg/kg, and the purified cumene with the organic acid impurity content of less than or equal to 50mg/kg is obtained after the alkali washing treatment of the fresh alkali liquor and the circulating alkali liquor of the alkali washing tower in the prior art, and other process data are shown in Table 1.
[ example 1 ]
As shown in fig. 1, this embodiment provides a method for alkaline washing a cumene raw material in a CHPPO apparatus, which specifically includes the following process flows: acid-containing cumene 11 containing organic acid impurities from the outside and return alkali liquor 23 pressurized by a water phase booster pump H are combined and enter a first mixer A, primary circulating alkali liquor 22 pressurized by a collector kettle liquid pump C also enters the first mixer A, an outflow primary mixed material 12 enters an aggregation separator B after oil-water mixing, an outflow collector oil phase 13 and fresh alkali liquor 28 from the outside are combined and enter a second mixer D after aggregation separation, a secondary circulating alkali liquor 25 pressurized by the water phase booster pump H also enters the second mixer D, a separator oil phase 15 pressurized by an oil phase booster pump E also enters the second mixer D, an outflow secondary mixed material 14 enters a hydrocyclone F after oil-water mixing, and an outflow hydrocyclone oil phase is taken as purified cumene 16 to be sent out of the outside after hydrocyclone separation. A part of the collector aqueous phase 24 flowing out of the collector-separator is pressurized by the collector still pump C and then enters the first mixer A as a circulating lye 22, and the other part of the collector aqueous phase is sent out as a waste lye 21. The hydrocyclone water phase 26 flowing out of the hydrocyclone enters an oil-water separator G, after oil-water separation, the outflow separator oil phase 15 enters a second mixer D after being pressurized by an oil phase booster pump E, one part of the separator water phase 27 flowing out of the oil-water separator enters the first mixer A as a return alkali liquor 23 after being pressurized by a water phase booster pump H, and the other part of the separator water phase 27 enters the second mixer D as a secondary circulating alkali liquor 25.
In the commercial industrial production device with nominal capacity of 5 ten thousand tons/year in the CHPPO apparatus of this embodiment, the parameters of the aggregation separator device in the main device are Φ 3000 × 11500mm, the unit weight of the device is 37000 kg, the parameters of the hydrocyclone separator device are Φ 2000 × 6300mm, the unit weight of the device is 14000 kg, the parameters of the oil-water separator device are Φ 2400 × 7500mm, the unit weight of the device is 18000 kg, and the total weight of 3 main devices is 69000 kg. The content of organic acid impurities in the acid-containing cumene from the outside is 120mg/kg, and after the alkaline washing treatment of the first mixer, the aggregation separator, the second mixer, the hydrocyclone separator and the oil-water separator in the embodiment, the purified cumene with the content of the organic acid impurities of less than or equal to 50mg/kg is obtained, and other process data are shown in Table 2. Compared with the comparative example 1, the weight of equipment steel can be saved by 41000 kg, the equipment engineering investment can be saved by 37.27 percent, and better technical effects can be achieved.
Comparative example 2
In the prior art, a conventional alkaline washing tower process flow is adopted to carry out alkaline washing treatment on an acid-containing cumene raw material, a CHPPO device is a commercial industrial production device with nominal capacity of 10 ten thousand tons/year, the equipment parameter of a main equipment alkaline washing tower is phi 4400 multiplied by 40000mm, and the equipment single weight is 163000 kg. The organic acid impurity content in the acid-containing cumene from the outside is 200-1000mg/kg, and the purified cumene with the organic acid impurity content of less than or equal to 50mg/kg is obtained after the alkali washing treatment of the fresh alkali liquor and the circulating alkali liquor of the alkali washing tower in the prior art, and other process data are shown in Table 1.
[ example 2 ]
In the same manner as in example 1, in a commercial industrial production plant in which only the nominal capacity of the CHPPO plant was changed to 10 ten thousand tons/year, the parameters of the aggregation separator equipment in the main equipment were Φ 4600 × 12200mm, the unit weight of the equipment was 59000 kg, the parameters of the hydrocyclone equipment were Φ 2800 × 6600mm, the unit weight of the equipment was 20000 kg, the parameters of the oil-water separator equipment were Φ 3200 × 8000mm, the unit weight of the equipment was 27000 kg, and the total weight of 3 main equipments was 106000 kg. The content of organic acid impurities in the acid-containing cumene from the outside is 4700mg/kg, and after the alkaline washing treatment of the first mixer, the aggregation separator, the second mixer, the hydrocyclone separator and the oil-water separator in the embodiment, the purified cumene with the content of the organic acid impurities of less than or equal to 50mg/kg is obtained, and other process data are shown in Table 2. Compared with the comparative example 2, the weight of the equipment steel can be saved by 57000 kg, the equipment engineering investment can be saved by 34.97 percent, and a better technical effect is achieved.
Comparative example 3
In the prior art, the acid-containing cumene raw material is subjected to alkaline washing by adopting a conventional alkaline washing tower process flow, a commercial industrial production device with a nominal capacity of a CHPPO device of 20 ten thousand tons/year is adopted, the equipment parameter of an alkaline washing tower of main equipment is phi 6000 multiplied by 44000mm, and the unit weight of the equipment is 254000 kg. The organic acid impurity content in the acid-containing cumene from the outside is 200-1000mg/kg, and the purified cumene with the organic acid impurity content of less than or equal to 50mg/kg is obtained after the alkali washing treatment of the fresh alkali liquor and the circulating alkali liquor of the alkali washing tower in the prior art, and other process data are shown in Table 1.
[ example 3 ]
In the same manner as in example 1, in a commercial industrial production plant in which only the nominal capacity of the CHPPO apparatus was changed to 20 ten thousand tons/year, the parameters of the aggregation separator device in the main equipment were Φ 6800 × 13400mm, the unit weight of the device was 100000 kg, the parameters of the hydrocyclone separator device were Φ 4000 × 7300mm, the unit weight of the device was 32000 kg, the parameters of the oil-water separator device were Φ 4600 × 8800mm, the unit weight of the device was 43000 kg, and the total weight of 3 main equipments was 175000 kg. The content of organic acid impurities in the acid-containing cumene from the outside is 340mg/kg, and after the alkaline washing treatment of the first mixer, the aggregation separator, the second mixer, the hydrocyclone separator and the oil-water separator in the embodiment, the purified cumene with the content of the organic acid impurities of less than or equal to 50mg/kg is obtained, and other process data are shown in Table 2. Compared with the comparative example 3, the weight of equipment steel can be saved by 79000 kg, the investment of equipment engineering can be saved by 31.10 percent, and a better technical effect is achieved.
Comparative example 4
In the prior art, a conventional alkaline washing tower process flow is adopted to carry out alkaline washing treatment on an acid-containing cumene raw material, a commercial industrial production device with a nominal capacity of a CHPPO (propylene oxide polymer) device of 40 ten thousand tons/year is adopted, equipment parameters of an alkaline washing tower of main equipment are 8800X 46000mm, and the unit weight of the equipment is 346000 kg. The organic acid impurity content in the acid-containing cumene from the outside is 200-1000mg/kg, and the purified cumene with the organic acid impurity content of less than or equal to 50mg/kg is obtained after the alkali washing treatment of the fresh alkali liquor and the circulating alkali liquor of the alkali washing tower in the prior art, and other process data are shown in Table 1.
[ example 4 ]
In the same way as [ example 1 ], only the nominal capacity of the CHPPO apparatus was changed to 40 ten thousand tons/year commercial industrial production apparatus, the parameters of the aggregation separator equipment in the main equipment were Φ 10000 × 14200mm, the unit weight of the equipment was 140000 kilograms, the parameters of the hydrocyclone separator equipment were Φ 5800 × 7800mm, the unit weight of the equipment was 43000 kilograms, the parameters of the oil-water separator equipment were Φ 6400 × 9300mm, the unit weight of the equipment was 57000 kilograms, and the total weight of 3 main equipments was 240000 kilograms. The content of organic acid impurities in the acid-containing cumene from the outside is 100mg/kg, and after the alkaline washing treatment of the first mixer, the aggregation separator, the second mixer, the hydrocyclone separator and the oil-water separator in the embodiment, the purified cumene with the content of the organic acid impurities of less than or equal to 50mg/kg is obtained, and other process data are shown in Table 2. Compared with the comparative example 4, 106000 kg of equipment steel weight can be saved, the equipment engineering investment can be saved by 30.64%, and a better technical effect is achieved.
Comparative example 5
In the prior art, a conventional alkaline washing tower process flow is adopted to carry out alkaline washing treatment on an acid-containing cumene raw material, a commercial industrial production device with a nominal capacity of a CHPPO device of 40 ten thousand tons/year is adopted, equipment parameters of an alkaline washing tower of main equipment are phi 8400X 46000mm, and the unit weight of the equipment is 423000 kg. The organic acid impurity content in the acid-containing cumene from the outside is 200-1000mg/kg, and the purified cumene with the organic acid impurity content of less than or equal to 50mg/kg is obtained after the alkali washing treatment of the fresh alkali liquor and the circulating alkali liquor of the alkali washing tower in the prior art, and other process data are shown in Table 1.
[ example 5 ]
In the same way as [ example 1 ], only the nominal capacity of the CHPPO apparatus was changed to 40 ten thousand tons/year commercial industrial production apparatus, the parameters of the aggregation separator device in the main apparatus were Φ 10000 × 14000mm, the unit weight of the apparatus was 1699000 kg, the parameters of the hydrocyclone separator device were Φ 5800 × 7600mm, the unit weight of the apparatus was 51000 kg, the parameters of the oil-water separator device were Φ 6400 × 9100mm, the unit weight of the apparatus was 69000 kg, and the total weight of 3 main apparatuses was 289000 kg. The content of organic acid impurities in the acid-containing cumene from the outside is 5000mg/kg, and after the alkaline washing treatment of the first mixer, the aggregation separator, the second mixer, the hydrocyclone separator and the oil-water separator in the embodiment, the purified cumene with the content of the organic acid impurities of less than or equal to 50mg/kg is obtained, and other process data are shown in Table 2. Compared with the comparative example 5, 134000 kg of equipment steel weight can be saved, 31.68% of equipment engineering investment can be saved, and a better technical effect is achieved.
Comparative example 6
In the prior art, a conventional alkaline washing tower process flow is adopted to carry out alkaline washing treatment on an acid-containing cumene raw material, a CHPPO device is a commercial industrial production device with nominal capacity of 80 ten thousand tons/year, the equipment parameters of a main equipment alkaline washing tower are phi 12000 multiplied by 50000mm, and the equipment single weight is 577000 kg. The organic acid impurity content in the acid-containing cumene from the outside is 200-1000mg/kg, and the purified cumene with the organic acid impurity content of less than or equal to 50mg/kg is obtained after the alkali washing treatment of the fresh alkali liquor and the circulating alkali liquor of the alkali washing tower in the prior art, and other process data are shown in Table 1.
[ example 6 ]
In the same manner as in example 1, in a commercial industrial production plant in which only the nominal capacity of the CHPPO apparatus was changed to 80 ten thousand tons/year, the parameters of the aggregation separator device in the main equipment were Φ 15200 × 15400mm, the unit weight of the device was 252000 kilograms, the parameters of the hydrocyclone separator device were Φ 8000 × 8400mm, the unit weight of the device was 73000 kilograms, the parameters of the oil-water separator device was Φ 9000 × 10000mm, the unit weight of the device was 97000 kilograms, and the total weight of 3 main devices was 422000 kilograms. The content of organic acid impurities in the acid-containing cumene from the outside is 3200mg/kg, and after the alkaline washing treatment of the first mixer, the aggregation separator, the second mixer, the hydrocyclone separator and the oil-water separator in the embodiment, the purified cumene with the content of the organic acid impurities of less than or equal to 50mg/kg is obtained, and other process data are shown in Table 2. Compared with the comparative example 6, 155000 kg of equipment steel weight can be saved, the equipment engineering investment can be saved by 26.86%, and a better technical effect is achieved.
Table 1 summary of process data for a prior art caustic tower
Table 2 summary of process data of the main apparatus of the invention
The embodiments of the present invention have been described in detail, but the embodiments are merely examples, and the present invention is not limited to the embodiments described above. It will be appreciated by those skilled in the art that any equivalent modifications and substitutions are within the scope of the present invention. Accordingly, equivalent changes and modifications made without departing from the spirit and scope of the present invention should be covered by the present invention.
Claims (9)
1. A method for washing a cumene raw material by an alkali in a CHPPO device is characterized by comprising the following steps: in a large-scale commercial CHPPO industrial production device with nominal capacity of 5-80 ten thousand tons/year, the method comprises the following process flows:
a) acid-containing cumene (11) containing organic acid impurities, primary circulating alkali liquor (22) pressurized by a collector kettle liquid pump (C) and return alkali liquor (23) pressurized by a water phase booster pump (H) are subjected to liquid drop dispersion, liquid-liquid contact, oil-water combination and full mixing in a first mixer (A), and the organic acid impurities in the acid-containing cumene (11) are subjected to neutralization reaction with the primary circulating alkali liquor (22) and the liquid alkali in the return alkali liquor (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, oil drop particles are aggregated to form a continuous oil phase by utilizing the characteristics of oleophylic hydrophobic materials, and meanwhile, the oil drop particles are aggregated to form a continuous water phase by utilizing the characteristics of oleophobic hydrophilic materials, so that oil-water layer separation is realized; the collector oil phase (13) is allowed to contain a small amount of water phase; the water phase of the collector does not allow oil-containing phase, one part of the water phase (24) of the collector is pressurized by a collector still pump (C) and then enters the first mixer (A) as a circulating alkali liquor (22), and the other part of the water phase (24) of the collector is sent out as a waste alkali liquor (21);
c) The collector oil phase (13) without completely removing organic acid impurities and the separator oil phase (15) after being pressurized by the oil phase booster pump (E) are dispersed, contacted with liquid and liquid in a second mixer (D) with liquid drops of fresh alkali liquor (28) from the outside and secondary circulating alkali liquor (25) after being pressurized by the water phase booster pump (H), oil and water are combined and fully mixed, and the organic acid impurities which are not completely removed in the collector oil phase (13) and the separator oil phase (15) and the liquid alkali in the fresh alkali liquor (28) and the secondary circulating alkali liquor (25) are removed through neutralization reaction;
d) the second mixed material (14) flowing out after the second mixer (D) is mixed by oil and water enters a hydrocyclone (F), and the oil phase and the water phase with different densities are gathered and separated by using the centrifugal force generated in the hydrocyclone (F) in the liquid rotating process; the hydrocyclone oil phase which flows out of the hydrocyclone (F) is not allowed to contain an aqueous phase and is sent out as purified cumene (16);
e) the 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 oil phase (15) flowing out of the hydrocyclone (F) is pressurized by an oil phase booster pump (E) and then returns to a second mixer (D); 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), wherein one part of the oil phase is returned to the first mixer (A) as the return alkali liquor (23), and the other part of the oil phase is returned to the second mixer (D) as the second circulating alkali liquor (25).
2. The method for alkaline washing of cumene raw materials by a CHPPO device according to claim 1, characterized in that ethylbenzene in the externally coming acid-containing cumene (11) is less than or equal to 0.60 wt%, propylbenzene is less than or equal to 0.30 wt%, butylbenzene is less than or equal to 0.10 wt%, and organic acid impurity content is 100-5000 mg/kg.
3. The method for alkaline washing of the cumene raw material by the CHPPO device as claimed in claim 2, wherein the acid-containing cumene (11) from outside is characterized in that ethylbenzene is less than or equal to 0.10 wt%, propylbenzene is less than or equal to 0.05 wt%, butylbenzene is less than or equal to 0.03 wt%, and the organic acid impurity content is 200-2000 mg/kg.
4. The method for washing cumene raw material with alkali by using a CHPPO device as claimed in claim 3, wherein the acid-containing cumene (11) from outside is characterized in that ethylbenzene is less than or equal to 0.01 wt%, propylbenzene is less than or equal to 0.01 wt%, butylbenzene is less than or equal to 0.01 wt%, and the organic acid impurity content is 500-1000 mg/kg.
5. The CHPPO plant caustic wash cumene feedstock of claim 1 wherein the first mixer (a) is operated at a pressure of 0.57-1.17MPaA and at an operating temperature of 25-85 ℃; said coalescing separator (B) operating at a pressure of 0.50 to 1.10MPaA and at a temperature of 25 to 85 ℃, said coalescing oil phase (13) being allowed to contain 2.0 to 9.0 wt% of an aqueous phase; the second mixer (D) operating at a pressure of 0.45-1.05MPaA and at a temperature of 25-85 ℃; the hydrocyclone (F) is operated at a pressure of 0.38-0.98MPaA and at a temperature of 25-85 ℃, and the hydrocyclone aqueous phase (26) is allowed to contain 2.0-9.0 wt% of 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 aqueous phase (27) is allowed to contain 2.0-9.0 wt% of an oil phase.
6. The method for alkaline washing of cumene feedstock in a CHPPO plant according to claim 5, characterized in that said first mixer (a) is operated at a pressure of 0.67-1.07MPaA and at a temperature of 35-75 ℃; said coalescing separator (B) operating at a pressure of 0.60 to 1.00MPaA and at a temperature of 35 to 75 ℃, said coalescing oil phase (13) being allowed to contain 3.0 to 8.0 wt% of an aqueous phase; said second mixer (D) operating at a pressure of 0.55-0.95MPaA and at a temperature of 35-75 ℃; the hydrocyclone (F) is operated at a pressure of 0.48-0.88MPaA and at a temperature of 35-75 ℃, and the hydrocyclone aqueous phase (26) is allowed to contain 3.0-8.0 wt% of oil phase; the oil-water separator (G) is operated at a pressure of 0.45-0.85MPaA and an operating temperature of 35-75 ℃, and the separator aqueous phase (27) is allowed to contain 3.0-8.0 wt% of an oil phase.
7. The method for alkaline washing of cumene feedstock in a CHPPO plant according to claim 6, characterized in that said first mixer (a) is operated at a pressure of 0.77-0.97MPaA and at a temperature of 45-65 ℃; said coalescing separator (B) operating at a pressure of 0.70 to 0.90MPaA and at a temperature of 45 to 65 ℃, said coalescing oil phase (13) being allowed to contain 4.0 to 7.0 wt% of an aqueous phase; the second mixer (D) is operated at a pressure of 0.65 to 0.85MPaA and at a temperature of 45 to 65 ℃; the hydrocyclone (F) is operated at a pressure of 0.58-0.78MPaA and a temperature of 45-65 ℃, and the hydrocyclone aqueous phase (26) is allowed to contain 4.0-7.0 wt% of oil phase; the oil-water separator (G) is operated at a pressure of 0.55-0.75MPaA and an operating temperature of 45-65 ℃, and the separator aqueous phase (27) is allowed to contain 4.0-7.0 wt% of an oil phase.
8. A system for caustic washing of a cumene feedstock in a CHPPO unit based on the method of any one of claims 1 to 7, comprising:
the first mixer (A);
the aggregation separator (B) is connected with the first mixer (A) through a pipeline;
the collector still pump (C) is connected with the collector separator (B) and the first mixer (A) through pipelines;
the second mixer (D) is connected with the aggregation separator (B) through a pipeline;
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;
and 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.
9. The system for washing cumene raw material with alkali of the CHPPO device according to claim 8, wherein the three layers of special materials in the aggregation separator (B) are sequentially composed of oleophilic hydrophobic material, oleophobic hydrophilic material and oleophilic hydrophobic material, wherein the oleophilic hydrophobic material is one of glass fiber, PET hollow fiber, PP hollow fiber and oil absorbent cotton fiber; the oleophobic hydrophilic material is modified fiber, composite fiber and TiO 2One material of nano fiber and absorbent cotton fiber.
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| CN112898238A (en) * | 2021-01-22 | 2021-06-04 | 中国石油化工股份有限公司 | CHPPO epoxidation reaction product crude separation system and separation method |
| CN112891977A (en) * | 2021-01-22 | 2021-06-04 | 中国石油化工股份有限公司 | CHPPO double-tower rectification separation system and separation method |
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