CN112898240A - CHPPO hydrocarbon injection crude separation system and crude separation method - Google Patents
CHPPO hydrocarbon injection crude separation system and crude separation method Download PDFInfo
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Abstract
The invention discloses a CHPPO hydrocarbon injection crude separation system and a crude separation method, wherein the crude separation system comprises a separation tower, a light component removal tower, a heavy component removal tower, an oil-water separator, a water scrubber and an extractor, the crude separation method injects organic hydrocarbons into the crude separation system, 10-80 wt% of organic hydrocarbons flow out of the top of the separation tower, 20-90 wt% of organic hydrocarbons flow out of the bottom of the separation tower, the temperature of the bottom of the separation tower is reduced to 70-110 ℃ from 150-210 ℃, and the increment of isopropylbenzene is reduced to 24-29 mg/kg from 2006-10177 mg/kg; and injecting water into a water scrubber and injecting cumene into an extractor to recover a small amount of propylene oxide and benzyl alcohol, so that the recovery rate of the propylene oxide is improved from 99.74-99.94 wt% to 99.95-99.97 wt%, and the problems of high temperature of a separation tower kettle, large cumene loss and low PO recovery rate in the prior art are solved.
Description
Technical Field
The invention relates to a system and a method for purifying propylene oxide by a CHPPO device, in particular to a crude separation system and a crude separation method for reducing the temperature of a tower kettle by injecting organic hydrocarbon in the rectification separation process of a crude propylene oxide separation tower of the CHPPO device.
Background
Propylene oxide PO is an important basic organic chemical raw material, contains a ternary cyclic ether structure and has high reaction activity. The largest uses of propylene oxide are in the production of polyether polyols, polyurethanes, propylene glycol, elastomers, adhesives, coatings and various types of nonionic surfactants. The major areas of propylene oxide production in the world today are in western europe, north america and asia. The annual demand of propylene oxide is expected to increase by about 4-8% in the future, wherein the demand of Asian markets increases rapidly, and especially in recent years, the consumption of propylene oxide in China and India markets is increased more rapidly than that in other countries. The annual demand of the propylene oxide for the next five to ten years can reach 1300-1500 ten thousand tons.
The industrial production method of propylene oxide mainly comprises chlorohydrin method, ethylbenzene co-oxidation method, hydrogen peroxide oxidation method, cumene oxidation method and the like. The production device of the chlorohydrin method has more waste residues and more waste water; the ethylbenzene co-oxidation production device has long process and high investment; the hydrogen peroxide oxidation method has large explosion risk of the production device; the cumene oxidation production device has the advantages of less three-waste discharge, strong product cost competitiveness, stability and safety, and is an optimal process route for the future large-scale production of the propylene oxide. At present, the CHPPO process by cumene oxidation is developed and patented by Sumitomo chemical company of Japan. The PDP process kit for preparing propylene oxide by the CHPPO method of 15 ten thousand tons/year has been independently developed and completed by the china petrochemical company limited, and is now performing the BED and DED engineering design for industrial application by the china petrochemical tianjin division.
Patent application No. 201510510737.2 discloses a method in which a propylene oxide solution is fed into a propylene oxide separation column for separation, and the separated aqueous solution containing a small amount of propylene oxide is fed into a propylene oxide re-separation column for re-separation.
Patent application No. 201510468132.1 discloses propylene oxide purification by employing a process comprising the steps of: a) contacting crude propylene oxide containing impurities with an alkali liquor to obtain a first material; b) contacting the first material with hydrazine or hydrazine hydrate to obtain a second material; c) the second material enters a low-pressure rectifying tower, a third material is obtained at the top of the tower, a recovered methanol material is obtained at the side line of the tower, and a heavy component material is obtained at the bottom of the tower; d) the third material enters a high-pressure rectifying tower, a fourth material is obtained at the tower top, and a propylene oxide product is obtained at the tower bottom; and the fourth material is recycled to the low-pressure rectifying tower. The method can be used in the industrial production of the purification of the propylene oxide.
Patent application No. 201410573617.2 discloses a method for purifying crude propylene oxide containing water, oxygen-containing compounds such as acetaldehyde, propionaldehyde and methanol, and hydrocarbon impurities such as propylene and 2-methylpentane, wherein the crude propylene oxide solution is subjected to a purification method combining multiple rectification and extractive rectification to obtain polymer-grade propylene oxide.
The three patents only adopt distillation rectification or adopt C7-C20 hydrocarbon as extracting agent for multiple extraction rectification, and the epoxy reaction product is separated to obtain the epoxypropane product.
Disclosure of Invention
The purpose of the invention is as follows: the invention aims to provide a crude separation system which adopts injected organic hydrocarbon to reduce the temperature of a tower kettle, reduce the loss of isopropyl benzene and improve the yield of propylene oxide in the rectification separation process of a CHPPO crude propylene oxide separation tower, and aims to provide a method for performing crude separation on epoxidation reactants by using the system.
The technical scheme is as follows: the CHPPO hydrocarbon injection crude separation system comprises a separation tower, a light component removal tower, a heavy component removal tower, an oil-water separator, a water scrubber and an extractor; the oil-water separator is respectively connected with the separation tower, the extractor and the water scrubber, and the extractor is respectively connected with the separation tower and the water scrubber.
The CHPPO hydrocarbon injection crude separation method comprises the following separation steps:
a. the epoxidation reaction product and organic hydrocarbon enter a separation tower, light reaction products and separation tower bottom liquid are obtained through separation, the light reaction products enter a light component removal tower, light components and heavy components of the light component removal tower are obtained through separation, the light components are sent out of the system, the heavy components of the light component removal tower enter a heavy component removal tower, crude PO products and heavy components containing hydrocarbon are obtained through separation, and the crude PO products and the heavy components containing hydrocarbon are respectively sent out of the system;
b. the residue in the separation tower enters an oil-water separator, and an oil-phase material and a water-phase material are obtained through separation; the oil phase material enters a water scrubber, water is used for extraction and washing to obtain water scrubbing liquid and water-containing benzyl alcohol, and the water-containing benzyl alcohol is sent out of the system;
c. mixing the water phase material with a washing liquid, adding an alkali solution, mixing and carrying out alkali washing to obtain circulating water; the circulating water enters an extractor, cumene is used for extraction to obtain extraction liquid and waste water, the waste water is sent out of the system, and the extraction liquid and the epoxidation reaction product are mixed and enter a separation tower.
Preferably, the process parameters of the crude separation method are as follows: the operating pressure of the separation tower is 0.12-0.25 MPaA, the operating temperature of the top of the tower is 41-77 ℃, and the operating temperature of the bottom of the tower is 70-110 ℃; the operating pressure of the light component removal tower is 0.26-0.39 MPaA, the operating temperature of the top of the tower is 39-79 ℃, and the operating temperature of the bottom of the tower is 51-91 ℃; the operating pressure of the de-heavy tower is 0.14-0.27 MPaA, the operating temperature of the tower top is 35-75 ℃, and the operating temperature of the tower kettle is 63-103 ℃; the operating pressure of the oil-water separator is 0.18-0.31 MPaA, and the operating temperature is 70-110 ℃; the operation pressure of the water scrubber is 0.16-0.29 MPaA, the operation temperature is 70-110 ℃, the extraction grade is 3-15 grades, and the solvent ratio is 2.0-10.0; the operating pressure of the extractor is 0.14-0.27 MPaA, the operating temperature is 70-110 ℃, the extraction grade number is 30-60 grades, and the solvent ratio is 0.4-8.8.
More preferably, the process parameters of the crude separation method are as follows: the operating pressure of the separation tower is 0.14-0.23 MPaA, the operating temperature of the top of the tower is 46-72 ℃, and the operating temperature of the bottom of the tower is 75-105 ℃; the operating pressure of the light component removal tower is 0.28-0.37 MPaA, the operating temperature of the top of the tower is 44-74 ℃, and the operating temperature of the bottom of the tower is 56-86 ℃; the operating pressure of the de-heavy tower is 0.16-0.25 MPaA, the operating temperature of the tower top is 40-70 ℃, and the operating temperature of the tower kettle is 68-98 ℃; the operating pressure of the oil-water separator is 0.20-0.29 MPaA, and the operating temperature is 75-105 ℃; the operation pressure of the water scrubber is 0.18-0.27 MPaA, the operation temperature is 75-100 ℃, the extraction grade is 5-13 grades, and the solvent ratio is 3.0-9.0; the operating pressure of the extractor is 0.16-0.25 MPaA, the operating temperature is 75-100 ℃, the number of extraction stages is 35-55, and the solvent ratio is 2.2-7.0.
Most preferably, the process parameters of the crude separation method are as follows: the operating pressure of the separation tower is 0.16-0.21 MPaA, the operating temperature of the top of the tower is 51-67 ℃, and the operating temperature of the bottom of the tower is 80-100 ℃; the operating pressure of the light component removal tower is 0.30-0.35 MPaA, the operating temperature of the top of the tower is 49-69 ℃, and the operating temperature of the bottom of the tower is 61-81 ℃; the operating pressure of the de-heavy tower is 0.18-0.23 MPaA, the operating temperature of the tower top is 45-65 ℃, and the operating temperature of the tower kettle is 73-93 ℃; the operating pressure of the oil-water separator is 0.22-0.27 MPaA, and the operating temperature is 80-100 ℃; the operation pressure of the water scrubber is 0.20-0.25 MPaA, the operation temperature is 80-90 ℃, the extraction stages are 7-11 stages, and the solvent ratio is 4.0-8.0; the operating pressure of the extractor is 0.18-0.23 MPaA, the operating temperature is 80-90 ℃, the number of extraction stages is 40-50, and the solvent ratio is 4.0-5.2.
In the separation step a, the organic hydrocarbon is one or more than one mixture of C5-C7 organic hydrocarbons.
The C5-C7 organic hydrocarbon is one or a mixture of more than one of cyclopentane, methyl pentane, methyl cyclopentane, n-hexane, isohexane, cyclohexane, methyl hexane, dimethyl butene, methyl pentene, hexene, heptene and benzene.
In the separation step a, the organic hydrocarbon injection position can be a separation tower, an oil-water separator, a water scrubber or an extractor.
In the separation step a, the light reaction product contains 10-80 wt% of organic hydrocarbon, and the bottom liquid of the separation tower contains 20-90 wt% of organic hydrocarbon.
In the separation step b, the water is one of primary desalted water, secondary desalted water, distilled water, refined water, purified water and pure water.
The inventor researches and discovers that in the process for preparing the propylene oxide in the prior art, a distillation rectification method or an extraction rectification method is mostly adopted to separate the epoxidation reaction product to obtain a crude propylene oxide product. The temperature of the rectifying tower is not controlled, the temperature of the tower kettle of the rectifying tower is high, and the cumene is easy to react to generate the cumene, so that the loss of the cumene is large, and the recovery rate of the propylene oxide product is low. Therefore, the invention aims to optimize the CHPPO epoxidation reaction product crude separation system and the process flow and solve the problems in the prior art.
Has the advantages that: compared with the prior art, the invention has the following remarkable advantages: in a CHPPO production device with nominal capacity of 5-90 ten thousand tons/annualized, in the process of rectifying, separating, purifying and refining an epoxidation reaction product into a crude propylene oxide product, injecting organic hydrocarbon, rectifying and separating the material in a separation tower, setting 10-80 wt% of the organic hydrocarbon to flow out of the top of the separation tower, and setting the remaining 20-90 wt% of the organic hydrocarbon to flow out of a tower kettle of the separation tower, so that the temperature of the tower kettle of the separation tower is reduced to 70-110 ℃ from 150-210 ℃ in the prior art, cumene is generated in the tower kettle of the separation tower and is reduced to 24-29 mg/kg from 2006-10177 mg/kg in the prior art; the oil-water separator is used for separating oil from water, water is injected into the water scrubber for water scrubbing, cumene is injected into the extractor for extraction, and a small amount of propylene oxide and benzyl alcohol are recovered, so that the recovery rate of the propylene oxide product in the separation tower is improved to 99.95-99.97 wt% from 99.74-99.94 wt% in the prior art, and a better technical effect is achieved.
Drawings
FIG. 1 is a process flow diagram of the present invention.
Detailed Description
The technical scheme of the invention is further explained by combining the attached drawings.
Example 1
Taking a CHPPO industrial device with the production scale of 5 ten thousand tons/year as an example, by adopting the CHPPO hydrocarbon injection crude separation system and the crude separation method, firstly, after low-boiling-point organic hydrocarbon 24 is introduced into a crude separation tower A1, the material is rectified and separated in a separation tower A1, so that the tower bottom temperature of the separation tower A1 is reduced, cumene is prevented from generating and cumene is prevented, and the cumene loss is reduced; secondly, an oil-water separator B1, a water scrubber B2 and an extractor B3 are arranged at the bottom of a separation tower A1, water 19 is injected into the water scrubber B2, isopropyl benzene 27 is injected into the extractor B3, a small amount of propylene oxide and benzyl alcohol are recovered, the recovery rate of a separation tower A1 propylene oxide product is improved, a crude PO tower is selected as the separation tower A1, and secondary salt water is removed as the water 19. The water 19 may be any one of primary desalted water, distilled water, refined water, purified water and pure water. The entry point for the organic hydrocarbons 24 may also be a splitter a1, a de-oiler B1, or a water scrubber B2.
As shown in fig. 1, the process flow of this embodiment is as follows: mixing a reaction product 11 from an external ring oxidation reaction unit of the system, which is subjected to propylene removal, with an extract liquid 26, then feeding the mixture into a crude PO tower, injecting organic hydrocarbon 24 from the outside of the system into the crude PO tower, rectifying and separating the materials, feeding a light reaction product 12 which does not contain water and contains a part of organic hydrocarbon and is produced at the top of the crude PO tower into a light component removal tower A2, and feeding a light component 23 flowing out of the tower top out of the system; the light component removal tower bottom liquid 13 flowing out of the tower bottom enters a heavy component removal tower A3, and a crude PO product 14 at the tower top and a hydrocarbon-containing heavy component 15 at the tower bottom are obtained and are respectively sent out of the system; the crude PO tower residue 16 containing the other part of organic hydrocarbon in the crude PO tower enters an oil-water separator B1 for oil-water separation to obtain an oil phase material flow 17 and a water phase material flow 18; the oil phase material flow 17 passes through a water scrubber B2, and is extracted and washed by secondary desalted water to obtain water scrubbing liquid 21 and hydrous benzyl alcohol 20 with a small amount of propylene oxide and water-soluble impurities removed, and the water scrubbing liquid and the hydrous benzyl alcohol 20 are sent out of the system; mixing the water phase material flow 18 and the water washing liquid 21, adding an alkali solution 22, removing trace acid media to form circulating water 25, feeding the circulating water into an extractor B3, performing liquid-liquid extraction by using cumene 27 from the outside of the system to obtain an extract 26 of recovered benzyl alcohol, mixing the extract 26 with a reaction product 11, returning the mixture to the crude PO tower, and sending raffinate serving as waste water 28 out of the system.
The process operating parameters of the embodiment are as follows: the low boiling organic hydrocarbon 24 was introduced into the crude PO column, 41.2 wt% of the organic hydrocarbon flowed out from the top of the crude PO column, 58.8 wt% of the organic hydrocarbon flowed out from the bottom of the crude PO column, and the organic hydrocarbon 24 was 100 wt% n-hexane. The operating pressure of the crude PO tower is 0.18MPaA, the operating temperature of the tower top is 52 ℃, and the operating temperature of the tower kettle is 86 ℃; the operating pressure of the lightness-removing column A2 is 0.30MPaA, the operating temperature of the top of the light-removing column is 54 ℃, and the operating temperature of the bottom of the light-removing column is 68 ℃; the operating pressure of the de-heavy tower A3 is 0.18MPaA, the operating temperature of the tower top is 48 ℃, and the operating temperature of the tower kettle is 76 ℃; the operating pressure of the oil-water separator B1 is 0.22MPaA, and the operating temperature is 86 ℃; the operation pressure of the water scrubber B2 is 0.20MPaA, the operation temperature is 86 ℃, the extraction stage number is 6 stages, and the solvent ratio is 8.2; the extractor B3 was operated at 0.18MPaA, 86 deg.C, 40 extraction stages and a solvent ratio of 5.6.
Therefore, by adopting the CHPPO hydrocarbon injection crude separation system and the crude separation method, the operation temperature of the tower bottom of the crude PO tower is reduced to 86 ℃, cumene generated in the tower bottom of the crude PO tower is led to be led to flow from 300mg/kg of inflow material to 326mg/kg of outflow material, the increment is 26mg/kg, the recovery rate of the epoxypropane product of the crude PO tower is improved to 99.96 wt%, and better technical effect is achieved.
Example 2
As in example 1, only the nominal capacity and process operating parameters were changed, the nominal capacity being changed to a 15-million ton/year CHPPO commercial industrial production plant, the process operating parameters being modified as follows: the low boiling organic hydrocarbon 24 was introduced into the crude PO column, 55.3 wt% of the organic hydrocarbon was taken out from the top of the crude PO column, 44.7 wt% of the organic hydrocarbon was taken out from the bottom of the crude PO column, and the organic hydrocarbon 24 was 100 wt% hexene. The operating pressure of the crude PO tower is 0.21MPaA, the operating temperature of the tower top is 65 ℃, and the operating temperature of the tower kettle is 94 ℃; the operating pressure of the lightness-removing column A2 is 0.35MPaA, the operating temperature of the top of the light-removing column is 63 ℃, and the operating temperature of the bottom of the light-removing column is 77 ℃; the operating pressure of the de-heavy tower A3 is 0.22MPaA, the operating temperature of the top of the tower is 61 ℃, and the operating temperature of the bottom of the tower is 89 ℃; the operating pressure of the oil-water separator B1 is 0.26MPaA, and the operating temperature is 94 ℃; the operation pressure of the water scrubber B2 is 0.24MPaA, the operation temperature is 94 ℃, the extraction stages are 12 stages, and the solvent ratio is 4.8; the extractor B3 was operated at a pressure of 0.22MPaA, an operating temperature of 94 deg.C, extraction stages of 52 stages, and a solvent ratio of 3.2.
Therefore, by adopting the CHPPO hydrocarbon injection crude separation system and the crude separation method, the operation temperature of the tower bottom of the crude PO tower is reduced to 94 ℃, cumene generated in the tower bottom of the crude PO tower is led to be flowed from 300mg/kg of the inflow material to 327mg/kg of the outflow material, the increment is 27mg/kg, the recovery rate of the propylene oxide product in the crude PO tower is improved to 99.96 wt%, and better technical effects are achieved.
Example 3
As in example 1, only the nominal capacity and process operating parameters were changed, the nominal capacity being changed to a 30-million ton/year CHPPO commercial industrial production plant, the process operating parameters being modified as follows: the low boiling organic hydrocarbon 24 was introduced into the crude PO column, 38.1 wt% of the organic hydrocarbon was taken overhead from the crude PO column, 61.9 wt% of the organic hydrocarbon was taken bottoms from the crude PO column, and the organic hydrocarbon 24 was a mixture of 90 wt% isohexane and 10 wt% methylpentane. The operating pressure of the crude PO tower is 0.15MPaA, the operating temperature of the tower top is 48 ℃, and the operating temperature of the tower kettle is 78 ℃; the operating pressure of the lightness-removing column A2 is 0.30MPaA, the operating temperature of the top of the light-removing column is 54 ℃, and the operating temperature of the bottom of the light-removing column is 68 ℃; the operating pressure of the de-heavy tower A3 is 0.18MPaA, the operating temperature of the tower top is 48 ℃, and the operating temperature of the tower kettle is 76 ℃; the operating pressure of the oil-water separator B1 is 0.22MPaA, and the operating temperature is 78 ℃; the operation pressure of the water scrubber B2 is 0.20MPaA, the operation temperature is 78 ℃, the extraction stage number is 6 stages, and the solvent ratio is 8.2; the extractor B3 was operated at 0.18MPaA, 78 deg.C, 40 extraction stages and a solvent ratio of 5.6.
Therefore, by adopting the CHPPO hydrocarbon injection crude separation system and the crude separation method, the operation temperature of the tower bottom of the crude PO tower is reduced to 78 ℃, cumene generated in the tower bottom of the crude PO tower is led to be led to flow from 300mg/kg of inflow material to 325mg/kg of outflow material, the increment is 25mg/kg, the recovery rate of the propylene oxide product in the crude PO tower is improved to 99.96 wt%, and better technical effects are achieved.
Example 4
As in example 1, only the nominal capacity and process operating parameters were changed, the nominal capacity being changed to a 90-ten-thousand ton/year CHPPO commercial industrial production plant, the process operating parameters being modified as follows: the low boiling organic hydrocarbon 24 was introduced into the crude PO column, 63.7 wt% of the organic hydrocarbon was taken out from the top of the crude PO column, 36.3 wt% of the organic hydrocarbon was taken out from the bottom of the crude PO column, and the organic hydrocarbon 24 was a mixture of 70 wt% cyclohexane and 30 wt% benzene. The operating pressure of the crude PO tower is 0.23MPaA, the operating temperature of the tower top is 72 ℃, and the operating temperature of the tower kettle is 102 ℃; the operating pressure of the lightness-removing column A2 is 0.30MPaA, the operating temperature of the top of the light-removing column is 54 ℃, and the operating temperature of the bottom of the light-removing column is 68 ℃; the operating pressure of the de-heavy tower A3 is 0.18MPaA, the operating temperature of the tower top is 48 ℃, and the operating temperature of the tower kettle is 76 ℃; the operating pressure of the oil-water separator B1 is 0.22MPaA, and the operating temperature is 102 ℃; the operation pressure of the water scrubber B2 is 0.20MPaA, the operation temperature is 102 ℃, the extraction stage number is 6 stages, and the solvent ratio is 8.2; the extractor B3 was operated at a pressure of 0.18MPaA, an operating temperature of 102 deg.C, extraction stages of 40 stages, and a solvent ratio of 5.6.
Therefore, by adopting the CHPPO hydrocarbon injection crude separation system and the crude separation method, the operation temperature of the tower bottom of the crude PO tower is reduced to 102 ℃, cumene generated in the tower bottom of the crude PO tower is led to be led to flow from 300mg/kg of inflow material to 328mg/kg of outflow material, the increment is 28mg/kg, the recovery rate of the epoxypropane product of the crude PO tower is improved to 99.96 wt%, and better technical effects are achieved.
Example 5
As in example 1, only the nominal capacity and process operating parameters were changed, the nominal capacity being changed to a 30-million ton/year CHPPO commercial industrial production plant, the process operating parameters being modified as follows: the low boiling organic hydrocarbon 24 was introduced into the crude PO column, 10.0 wt% of the organic hydrocarbon flowed out of the top of the crude PO column, 90.0 wt% of the organic hydrocarbon flowed out of the bottom of the crude PO column, and the organic hydrocarbon 24 was 100 wt% cyclopentane. The operating pressure of the crude PO tower is 0.12MPaA, the operating temperature of the tower top is 41 ℃, and the operating temperature of the tower kettle is 70 ℃; the operating pressure of the lightness-removing column A2 is 0.26MPaA, the operating temperature of the top of the light-removing column is 39 ℃, and the operating temperature of the bottom of the light-removing column is 51 ℃; the operating pressure of the de-heavy tower A3 is 0.14MPaA, the operating temperature of the top of the tower is 35 ℃, and the operating temperature of the bottom of the tower is 63 ℃; the operating pressure of the oil-water separator B1 is 0.18MPaA, and the operating temperature is 70 ℃; the operation pressure of the water scrubber B2 is 0.16MPaA, the operation temperature is 70 ℃, the extraction stage number is 3 stages, and the solvent ratio is 10.0; the extractor B3 was operated at 0.14MPaA, 70 deg.C, 30 extraction stages and a solvent ratio of 8.8.
Therefore, by adopting the CHPPO hydrocarbon injection crude separation system and the crude separation method, the operation temperature of the tower bottom of the crude PO tower is reduced to 70 ℃, cumene generated in the tower bottom of the crude PO tower is led to be led to flow from 300mg/kg of inflow material to 324mg/kg of outflow material, the increment is 24mg/kg, the recovery rate of the propylene oxide product in the crude PO tower is improved to 99.97 wt%, and better technical effects are achieved.
Example 6
As in example 1, only the nominal capacity and process operating parameters were changed, the nominal capacity being changed to a 30-million ton/year CHPPO commercial industrial production plant, the process operating parameters being modified as follows: the lower boiling organic 24 hydrocarbons were introduced into the crude PO column, 80.0 wt% of the organic hydrocarbons flowed out of the top of the crude PO column, 20.0 wt% of the organic hydrocarbons flowed out of the bottom of the crude PO column, and the organic hydrocarbons 24 was 100 wt% heptene. The operating pressure of the crude PO tower is 0.25MPaA, the operating temperature of the tower top is 77 ℃, and the operating temperature of the tower kettle is 110 ℃; the operating pressure of the lightness-removing column A2 is 0.39MPaA, the operating temperature of the top of the light-removing column is 79 ℃, and the operating temperature of the bottom of the light-removing column is 91 ℃; the operating pressure of the de-heavy tower A3 is 0.27MPaA, the operating temperature of the tower top is 75 ℃, and the operating temperature of the tower kettle is 103 ℃; the operating pressure of the oil-water separator B1 is 0.31MPaA, and the operating temperature is 110 ℃; the operation pressure of the water scrubber B2 is 0.29MPaA, the operation temperature is 110 ℃, the extraction stage number is 15 stages, and the solvent ratio is 2.0; the extractor B3 was operated at 0.27MPaA, 110 deg.C, 60 extraction stages and a solvent ratio of 0.4.
Therefore, by adopting the CHPPO hydrocarbon injection crude separation system and the crude separation method, the operation temperature of the tower bottom of the crude PO tower is reduced to 110 ℃, cumene generated in the tower bottom of the crude PO tower is led to be led to flow from 300mg/kg of material inflow to 329mg/kg of material outflow, the increment is 29mg/kg, the recovery rate of the epoxypropane product in the crude PO tower is improved to 99.95 wt%, and better technical effects are achieved.
Comparative examples 1 to 6
Comparative examples 1 to 6 were set, and in a commercial industrial production plant of CHPPO having a nominal capacity of 30 ten thousand tons/year, no organic hydrocarbon and water were injected in the process flow, the operating temperature of the crude PO column bottom was 150 to 210 ℃, the process steps and other process parameters were the same as in example 3, whereby cumene formation and cumene formation in the crude PO column bottom resulted from the 300mg/kg of the feed inflow to 2306 to 10477mg/kg of the feed outflow, and the propylene oxide product recovery rate of the crude PO column was 99.74 to 99.94 wt%, as shown in Table 1.
TABLE 1 Table of cumene increment and propylene oxide recovery rate by changing the temperature of the crude PO column
Comparative examples 7 to 12
Comparative examples 7 to 12 were set, and in a commercial industrial production plant of CHPPO having a nominal capacity of 30 ten thousand tons/year, no organic hydrocarbon and water were injected in the process flow, the operating pressure of the crude PO column was 0.12 to 0.25MPaA, and the process steps and other process parameters were the same as those in example 3, whereby cumene formation and cumene formation in the bottom of the crude PO column resulted in cumene from 300mg/kg of the feed inflow to 2306 to 10477mg/kg of the feed outflow, and the propylene oxide product recovery of the crude PO column was 99.74 to 99.94 wt%, as shown in Table 2.
TABLE 2 Table of cumene increment and propylene oxide recovery rate by changing crude PO column pressure
Comparative examples 13 to 18
Comparative examples 13 to 18 were set, and in a commercial industrial production plant of CHPPO having a nominal capacity of 5 to 90 ten thousand tons/year, no organic hydrocarbon and water were injected in the process flow, the operating temperature of the crude PO column bottom was 202 ℃, the process steps and other process parameters were the same as in example 3, whereby cumene production and cumene formation in the crude PO column bottom was caused to be carried out from 300mg/kg of the inflow of the material to 7809 to 7815mg/kg of the outflow of the material, and the recovery rate of the propylene oxide product in the crude PO column was 99.82 to 99.89 wt%, see Table 3.
TABLE 3 cumene increment and propylene oxide recovery rate table for changing nominal capacity of CHPPO industrial production unit
Claims (9)
1. A CHPPO hydrocarbon injection crude separation system is characterized in that: comprises a separation tower (A1), a light component removal tower (A2), a heavy component removal tower (A3), an oil-water separator (B1), a water scrubber (B2) and an extractor (B3); the light component removal tower (A2) is connected with a separation tower (A1) and a heavy component removal tower (A3) respectively, the oil-water separator (B1) is connected with the separation tower (A1), the extractor (B3) and the water scrubber (B2) respectively, and the extractor (B3) is connected with the separation tower (A1) and the water scrubber (B2) respectively.
2. A CHPPO hydrocarbon injection crude separation method is characterized by comprising the following steps:
a. an epoxidation reaction product (11) and organic hydrocarbon (24) enter a separation tower (A1) and are separated to obtain a light reaction product (12) and a separation tower bottom liquid (16), the light reaction product (12) enters a light component removal tower (A2) and is separated to obtain a light component (23) and a heavy component removal tower (13), the light component (23) is sent out of the system, the heavy component removal tower (13) enters a heavy component removal tower (A3), and a crude PO product (14) and a heavy component containing hydrocarbon (15) are obtained by separation and are respectively sent out of the system;
b. the separation tower bottom liquid (16) enters an oil-water separator (B1) to be separated to obtain an oil phase material (17) and a water phase material (18); the oil phase material (17) enters a water scrubber (B2) and is extracted and washed by water (19) to obtain water scrubbing liquid (21) and water-containing benzyl alcohol (20), and the water-containing benzyl alcohol (20) is sent out of the system;
c. mixing the water phase material (18) with a water washing liquid (21), adding an alkali solution (22) for mixing and alkali washing to obtain circulating water (25); the recycling water (25) enters an extractor (B3), cumene (27) is used for extraction to obtain an extraction liquid (26) and waste water (28), the waste water (28) is sent out of the system, and the extraction liquid (26) and the epoxidation reaction product (11) are mixed and enter a separation tower (A1).
3. The CHPPO hydrocarbon injection crude separation method as claimed in claim 2, characterized in that: the operating pressure of the separation tower (A1) is 0.12-0.25 MPaA, the operating temperature of the top of the tower is 41-77 ℃, and the operating temperature of the bottom of the tower is 70-110 ℃; the operating pressure of the light component removal tower (A2) is 0.26-0.39 MPaA, the operating temperature of the top of the tower is 39-79 ℃, and the operating temperature of the bottom of the tower is 51-91 ℃; the operation pressure of the heavy component removing tower (A3) is 0.14-0.27 MPaA, the operation temperature of the tower top is 35-75 ℃, and the operation temperature of the tower kettle is 63-103 ℃.
4. The CHPPO hydrocarbon injection crude separation method as claimed in claim 2, characterized in that: the operating pressure of the oil-water separator (B1) is 0.18-0.31 MPaA, and the operating temperature is 70-110 ℃; the operation pressure of the water scrubber (B2) is 0.16-0.29 MPaA, the operation temperature is 70-110 ℃, the extraction stage number is 3-15, and the solvent ratio is 2.0-10.0; the operating pressure of the extractor (B3) is 0.14-0.27 MPaA, the operating temperature is 70-110 ℃, the number of extraction stages is 30-60, and the solvent ratio is 0.4-8.8.
5. The CHPPO hydrocarbon injection crude separation method as claimed in claim 2, characterized in that: in the step a, the organic hydrocarbon (24) is one or more than one mixture of C5-C7 organic hydrocarbons.
6. The CHPPO hydrocarbon injection crude separation method as claimed in claim 5, characterized in that: the C5-C7 organic hydrocarbon is one or a mixture of more than one of cyclopentane, methyl pentane, methyl cyclopentane, n-hexane, isohexane, cyclohexane, methyl hexane, dimethyl butene, methyl pentene, hexene, heptene and benzene.
7. The CHPPO hydrocarbon injection crude separation method as claimed in claim 2, characterized in that: in step a, the injection position of the organic hydrocarbon (24) can be a separation tower (A1), an oil-water separator (B1), a water scrubber (B2) or an extractor (B3).
8. The CHPPO hydrocarbon injection crude separation method as claimed in claim 2, characterized in that: in the step a, the light reaction product (12) contains 10-80 wt% of organic hydrocarbon, and the separation tower bottom liquid (16) contains 20-90 wt% of organic hydrocarbon.
9. The CHPPO hydrocarbon injection crude separation method as claimed in claim 2, characterized in that: in the step b, the water (19) is one of primary desalted water, secondary desalted water, distilled water, refined water, purified water and pure water.
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