CN109851587B - Method for producing butylene oxide - Google Patents
Method for producing butylene oxide Download PDFInfo
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- CN109851587B CN109851587B CN201711241136.1A CN201711241136A CN109851587B CN 109851587 B CN109851587 B CN 109851587B CN 201711241136 A CN201711241136 A CN 201711241136A CN 109851587 B CN109851587 B CN 109851587B
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Abstract
The invention relates to a production method of butylene oxide, which mainly solves the problems of low purity of an extracting agent, high loss, low yield of butylene oxide and high energy consumption caused by accumulation of heavy glycol component impurities in the prior art. The process comprises the steps of separating a stream comprising butylene oxide, an extractant, and a glycol in a separation column; the separation column is operated under conditions sufficient for the extractant and glycol to form an azeotrope, and a stream containing the extractant and glycol azeotrope is withdrawn in the separation column sidedraw. The method can be used in the industrial production of butylene oxide.
Description
Technical Field
The invention relates to a production method of epoxy butane, in particular to a purification method for extracting, rectifying and recovering an extracting agent from epoxy butane.
Background
1, 2-Butylene Oxide (BO) and Ethylene Oxide (EO) and Propylene Oxide (PO) homologues with molecular formula C4H8O (CAS number: 106-88-7), a substance with a three-membered ring structure, is chemically active and is mainly used as an intermediate for polyether polyol monomers and other synthetic materials. The 1, 2-butylene oxide can also be used for preparing foam plastics, synthetic rubber, nonionic surfactants and the like, can also be used as a diluent of nitrolacquer instead of acetone, and can also be used as a standard substance for chromatographic analysis.
As the olefin epoxide, butylene oxide has a larger amount of-CH in its molecular structure than ethylene oxide and propylene oxide2Functional groups, which, when used as monomers for the synthesis of polyether polyols, give products with excellent hydrophobic properties, and are particularly suitable for the outer surface waterproofing of certain demanding buildings and equipment. Meanwhile, the polyurethane material synthesized by copolymerization with the epoxy butane as a monomer has excellent cold resistanceIs not suitable for regions with severe cold climate.
The butylene oxide product has strict requirements on water, aldehyde and isomers, the water can influence the hydroxyl value and the foaming performance of the polymer, the aldehyde content is an environment-friendly requirement, and the isomers are end capping agents of long polymer chains, so that the product purity is strictly required in national standards and enterprise standards.
The quality and purity requirements of the qualified 1, 2-butylene oxide product in BASF enterprise standards are as follows: more than or equal to 99.5 percent of butylene oxide, less than or equal to 0.2 percent of butylene oxide isomer, less than or equal to 0.05 percent of total aldehyde and less than or equal to 0.03 percent of water.
The quality and purity requirements of the 1, 2-epoxybutane superior products are as follows: more than or equal to 99.9 percent of butylene oxide, less than or equal to 0.1 percent of butylene oxide isomer, less than or equal to 0.015 percent of total aldehyde and less than or equal to 0.005 percent of water.
The crude butylene oxide produced by the reaction usually contains impurities such as water, methanol, acetone, methyl formate and the like, and because the impurities form an azeotrope with the butylene oxide or the relative volatility is close to 1, the common rectification can not reach the standards of the butylene oxide product. In order to obtain high-purity butylene oxide satisfying the polymerization requirements, it is necessary to separate and remove impurities contained in butylene oxide.
The purification of butylene oxide generally adopts C7-C20 straight-chain and branched-chain hydrocarbons and (or) glycols as an extracting agent. For economic reasons, the purification of butylene oxide uses a mixture of linear and branched alkanes of C8 as extractant. The addition of the extractant increases the relative volatility of acetaldehyde, water, methanol and methyl formate to epoxybutane, and the acetaldehyde, water, methanol and methyl formate are removed from the top of the tower.
In the butylene epoxidation reaction product, 1, 2-epoxybutane and isomers thereof such as 1, 4-epoxybutane, 2, 3-epoxybutane and epoxyisobutane are mainly used, and in the epoxybutane refining process, the 1, 2-epoxybutane and isomers thereof are inevitably hydrolyzed to generate 1, 2-butanediol and corresponding diol due to the existence of water, and the hydrolysis reaction is continuously carried out with the time. If the diol in the extractant is not separated and removed, the diol in the extractant can be continuously accumulated, so that the content of the diol in the recycled extractant is too high, and the extraction effect of the extractant can be reduced until the extraction effect is lost. However, most of the glycols are soluble in water and also in organic solvents such as butylene oxide, and the removal efficiency by washing with water during the liquid-liquid phase separation is low, and the hydrolysis of butylene oxide is also accelerated. Moreover, since the boiling point of the glycol is higher than that of the C8 hydrocarbon, when the extractant is recycled in the system, the extractant and the extractant are cumulatively recycled, thereby reducing the extraction effect of the extractant. Therefore, it is very necessary to reduce the concentration of the glycol in the extractant. For example, document US4402794 discloses a single extractive rectification separation of impurities such as water, methanol, acetone, methyl formate and the like contained in a crude 1, 2-butylene oxide solution using C7-C9 hydrocarbons, preferably n-octane, as extractant. The organic layer obtained after layering by the phase separator at the top of the extractive distillation tower is sent to a rectifying tower to distill and separate methanol, acetone and the like; feeding the material flow in the bottom of the extractive distillation tower into an extractive distillation tower; and discharging the tower bottom liquid of the extraction and rectification tower. The method reduces the accumulation of the extractant in the extractant by discharging part of the tower bottom liquid containing the extractant and the 1, 2-butanediol. Because the content of 1, 2-butanediol in partial material flow discharged from the tower bottom is low, a large amount of extractant needs to be discharged to ensure the purity of the extractant, and a large amount of extractant is lost.
Document US4772732 discloses a process for purifying butene oxide by using an anion exchange resin and an adsorbent. The anion exchange resin removes acid and dehydrogenation impurities, while the adsorbent removes water from impurities of butylene oxide. The purification steps may be carried out individually or in combination, depending on the impurity content, and the process may be carried out batchwise in a reactor or continuously in a column or column. The ion exchange resin selected is a sulfonated macroreticular anion exchange resin and the adsorbent is a molecular sieve. The method has high cost, troublesome adsorption and analysis process and low treatment capacity.
The current situation of the prior art is that a method for producing the epoxybutane with low extractant loss, high purity, high epoxybutane yield and low energy consumption is still needed.
Disclosure of Invention
The present inventors have assiduously studied on the basis of the prior art and have found that at least one of the aforementioned problems can be solved by forming an azeotrope using an extracting agent and a heavy glycol component impurity and withdrawing the azeotrope from the side line of a separation column, and have thus completed the present invention.
In particular, the invention relates to a method for producing epoxybutane. The process comprises the steps of separating a stream comprising butylene oxide, an extractant, and a glycol in a separation column;
the separation column is operated under conditions sufficient for the extractant and the diol to form an azeotrope, and
a stream containing the extractant and glycol azeotrope is taken off the side of the separation column.
According to one aspect of the invention, the conditions sufficient for the extractant and the glycol to form an azeotrope comprise: the pressure is 0.02-0.40 MPaA, preferably 0.10-0.20 MPaA; the temperature of the azeotrope is 80-180 ℃, and preferably 120-150 ℃.
According to one aspect of the invention, the number of theoretical plates of the separation column is 15 to 80, preferably 20 to 65, and more preferably 20 to 50.
According to one aspect of the invention, the side line of the separation tower takes out the azeotrope at the position of 1 st to 8 th theoretical plates, preferably 2 nd to 6 th theoretical plates, and more preferably 2 th to 4 th theoretical plates above the reboiler return opening at the bottom of the separation tower.
According to one aspect of the invention, the ratio of the extracting agent to the butylene oxide in the stream containing the butylene oxide, the extracting agent and the glycol is (2-25): 1, preferably (3-20): 1, and more preferably (5-13): 1 in weight percentage.
According to one aspect of the invention, the stream comprising butylene oxide, extractant and glycol is derived from an extracted product stream obtained after extractive distillation of an olefin epoxidation reaction product.
According to one aspect of the invention, the diol comprises a hydrolysate of butylene oxide and/or isomers thereof.
The invention has the beneficial effects that: the method of the invention utilizes the extractant and the heavy glycol component impurities to form an azeotrope, and the azeotrope is extracted from the side line of the separation tower, so that the heavy glycol component impurities are discharged from the extractant circulating system, the circulating extractant is purified, the purity of the extractant is improved, the loss and the energy consumption of the extractant are reduced, and the yield of the epoxybutane is improved. Compared with the scheme that the material flow part in the tower kettle of the separation tower is directly discharged, the purity of the extracting agent is improved by 0.1-2%, the loss of the extracting agent is 0.1-1.3%, the energy consumption is reduced by 1-10%, and the yield of the epoxy butane is improved by 0.5-5%.
Drawings
FIG. 1 is a schematic flow diagram of the process of the present invention.
Fig. 2 is a schematic flow diagram of a process described in prior art document US 4402794.
In the drawings, like parts are provided with like reference numerals. The drawings are not to scale.
Description of reference numerals:
1 feed stream
2 extractant stream
3 butylene oxide product stream
4 reboiler feed stream
6 stream containing extractant and glycol azeotrope
A separation tower
B reboiler
The invention is described in detail below with reference to the drawings, but it is to be noted that the scope of the invention is not limited thereto, but is defined by the appended claims.
All publications, patent applications, patents, and other references mentioned in this specification are herein incorporated by reference in their entirety. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art. In case of conflict, the present specification, including definitions, will control.
When the specification concludes with claims with the heading "known to those skilled in the art", "prior art", or the like, to derive materials, substances, methods, procedures, devices, or components, etc., it is intended that the subject matter derived from the heading encompass those conventionally used in the art at the time of filing this application, but also include those that are not currently in use, but would become known in the art to be suitable for a similar purpose.
In the context of the present specification, anything or things which are not mentioned, except where explicitly stated, are directly applicable to those known in the art without any changes. Moreover, any embodiment described herein may be freely combined with one or more other embodiments described herein, and the technical solutions or concepts resulting therefrom are considered part of the original disclosure or original disclosure of the invention, and should not be considered as new matters not disclosed or contemplated herein, unless a person skilled in the art would consider such a combination to be clearly unreasonable.
Unless otherwise expressly indicated, all percentages, parts, ratios, etc. mentioned in this specification are by weight unless otherwise not in accordance with the conventional knowledge of those skilled in the art.
All pressures mentioned in this specification are absolute pressures unless explicitly stated.
The feedstock used in the process of the present invention is a stream comprising butylene oxide and an extractant. This stream is derived from the extract product stream obtained after extractive distillation of the olefin epoxidation reaction product in an extractive distillation column (not shown in the drawing). The purified extractant obtained in the method can be returned to the extraction and rectification tower for recycling.
The use of extractive agents for the purification of butylene oxide is well known. Generally, C7-C20 straight-chain and branched-chain hydrocarbons and/or glycols are used as the extractant. For economic reasons, mixtures of C8 linear and branched alkanes are used as extractants, for example n-octane, isooctane, 2-methyl-heptane. From the viewpoint of reducing the cost of the extractant, it is preferable to select a mixture.
According to the invention, in FIG. 1, a stream 1 containing butylene oxide, extractant and glycol is fed to a separation column A, a butylene oxide product stream 3 is removed from the top of the separation column, an extractant stream 2 is removed from the bottom of the separation column, and the removed extractant can be returned to a preceding extractive rectification column (not shown in the drawing) for recycling. The bottom of the separation tower A is provided with a reboiler B, the reboiler B is used for feeding tower bottom liquid into the reboiler B for heating to obtain a reboiler B discharge material flow 5 which is fed back to the lower part of the separation tower A, and a material flow 6 containing an extractant and glycol azeotrope is extracted from the side line of the separation tower A, so that glycol is discharged from the system.
According to the invention, the side draw of the separation tower selects a glycol enrichment position, and the position of the azeotrope is located on 1 st to 8 th theoretical plates, preferably 2 nd to 6 th theoretical plates, and more preferably 2 th to 4 th theoretical plates above a reboiler return opening at the bottom of the separation tower. At this point, the diol content was highest and the amount of butylene oxide entrained was the least in the azeotrope composition. The higher the butylene oxide concentration in the azeotrope composition, and the lower the diol concentration, the more butylene oxide is carried over when the azeotrope is taken and the greater the loss.
According to the present invention, the conditions sufficient for the extractant and the diol to form an azeotrope include: the pressure is 0.02-0.40 MPaA, the operation pressure is reduced as much as possible to reduce the requirement of equipment materials under the condition that the gas phase of the epoxy butane at the top of the tower adopts cooling water as a cooling medium and the operation pressure is met, the pressure is preferably 0.10-0.20 MPaA, and the temperature of an azeotrope is 80-180 ℃, and is preferably 120-150 ℃.
Taking 1, 2-butanediol as an example, the diol content of the azeotrope increases with increasing pressure, with a pressure of 3.63 wt% for 0.06MPaA, 4.90 wt% for 0.10MPaA, 6.16 wt% for 0.15MPaA, and 7.21 wt% for 0.20 MPaA. The higher the content of the diol in the azeotrope, the more diol is recovered and the less extractant is lost under the condition of the same side-draw amount. However, as the top of the tower is butylene oxide, the temperature of the butylene oxide exceeds 120 ℃, side reactions such as polymerization and the like can occur, the yield of the butylene oxide is reduced, meanwhile, the higher the temperature of the tower kettle is, the higher the requirement on the steam grade is, the comprehensive consideration is that 0.10-0.20 MPaA is preferred, and the temperature of the corresponding azeotrope is 120-150 ℃.
It should be noted that, regarding the concentration of the diol in the stream containing butylene oxide, the extractant and the diol, since 1, 2-butylene oxide and isomers thereof are continuously hydrolyzed in the presence of water to produce 1, 2-butylene glycol and the corresponding diol in the refining process, the concentration thereof is continuously increased as the hydrolysis reaction is continuously carried out.
FIG. 2 shows the prior art, wherein a stream 1 containing butylene oxide, an extractant and glycol enters a separation tower A, a butylene oxide product stream 3 is removed from the top of the separation tower A, an extractant stream 2 is removed from the bottom of the separation tower A, the bottom of the separation tower A is provided with a reboiler B, a reboiler B feed stream 4 feeds a tower bottom into the reboiler B for heating to obtain a reboiler B discharge stream 5, the reboiler B discharge stream is fed into the lower part of the separation tower C, and the extractant stream 2 is separated into a stream 6, so that the glycol is discharged out of the system. A greater amount of extractant is lost due to the reduction of glycol accumulation in the extractant by venting a portion of the bottoms stream.
The invention is further illustrated by the following specific embodiments.
Detailed Description
[ example 1 ]
According to the process flow shown in FIG. 1, the extracting agent is n-octane, the ratio of the extracting agent to the 1, 2-butylene oxide is 12:1 in weight percent in the material flow containing the 1, 2-butylene oxide, the extracting agent and the glycol, the number of theoretical plates of the separation tower is 30, and the side line extraction of the separation tower is positioned on the 2 nd theoretical plate above the reboiler return opening. The operating pressure of the separation tower is 0.10MPaA, the temperature is 68 ℃, the azeotropic temperature of the side-draw azeotrope is 129 ℃, the glycol content is 5.44 wt%, and the side-draw glycol is enriched and drawn.
The purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.95%, the recovery rate is 99.81%, the purity of the extractant at the bottom of the separation tower is 98.45%, and the loss of the extractant is 0.85%.
[ example 2 ]
According to the process flow diagram shown in FIG. 1, the extracting agent is n-octane, the ratio of the extracting agent to 1, 2-butylene oxide in the material flow containing 1, 2-butylene oxide, the extracting agent and glycol is 11:1 in percentage by weight, the number of theoretical plates of the separation tower is 30, and the side line extraction of the separation tower is positioned on the 2 nd theoretical plate above the reboiler return port. The operating pressure of the separation tower is 0.10MPaA, the temperature is 68 ℃, the azeotropic temperature of the side-draw azeotrope is 129 ℃, the glycol content is 5.44 wt%, and the side-draw glycol is enriched and drawn.
The purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.95%, the recovery rate is 99.83%, the purity of the extractant at the bottom of the separation tower is 98.51%, and the loss of the extractant is 0.90%.
[ example 3 ]
According to the process flow diagram shown in FIG. 1, the extracting agent is n-octane, the ratio of the extracting agent to 1, 2-butylene oxide in the material flow containing 1, 2-butylene oxide, the extracting agent and glycol is 10:1 in percentage by weight, the number of theoretical plates of the separation tower is 30, and the side line extraction of the separation tower is positioned on the 2 nd theoretical plate above the reboiler return port. The operating pressure of the separation tower is 0.10MPaA, the temperature is 68 ℃, the azeotropic temperature of the side-draw azeotrope is 129 ℃, the glycol content is 5.44 wt%, and the side-draw glycol is enriched and drawn.
The purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.94%, the recovery rate is 99.84%, the purity of the extractant at the bottom of the separation tower is 98.55%, and the loss of the extractant is 0.93%.
[ example 4 ]
According to the process flow diagram shown in FIG. 1, the extracting agent is n-octane, the ratio of the extracting agent to 1, 2-butylene oxide in the material flow containing 1, 2-butylene oxide, the extracting agent and glycol is 8:1 in percentage by weight, the number of theoretical plates of the separation tower is 30, and the side line extraction of the separation tower is positioned on the 2 nd theoretical plate above the reboiler return port. The operating pressure of the separation tower is 0.10MPaA, the temperature is 68 ℃, the azeotropic temperature of the side-draw azeotrope is 129 ℃, the glycol content is 5.44 wt%, and the side-draw glycol is enriched and drawn.
The purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.95%, the recovery rate is 99.88%, the purity of the extractant at the bottom of the separation tower is 98.23%, and the loss of the extractant is 0.94%.
[ example 5 ]
According to the process flow diagram shown in FIG. 1, the extracting agent is n-octane, the ratio of the extracting agent to the 1, 2-butylene oxide in the material flow containing the 1, 2-butylene oxide, the extracting agent and the glycol is 6:1 in percentage by weight, the number of theoretical plates of the separation tower is 30, and the side line extraction of the separation tower is positioned on the 2 nd theoretical plate above the reboiler return port. The operating pressure of the separation tower is 0.10MPaA, the temperature is 68 ℃, the azeotropic temperature of the side-draw azeotrope is 129 ℃, the glycol content is 5.44 wt%, and the side-draw glycol is enriched and drawn.
The purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.95%, the recovery rate is 99.87%, the purity of the extractant at the bottom of the separation tower is 98.02%, and the loss of the extractant is 0.97%.
[ example 6 ]
According to the process flow diagram shown in FIG. 1, the extractant is a C8 saturated alkane mixture, the ratio of the extractant to the 1, 2-butylene oxide in the stream containing the 1, 2-butylene oxide, the extractant and the glycol is 6:1 in percentage by weight, the theoretical plate number of the separation tower is 30, and the side draw of the separation tower is located on the 2 nd theoretical plate above the reboiler return port. The operating pressure of the separation tower is 0.10MPaA, the temperature is 68 ℃, the azeotropic temperature of the side-draw azeotrope is 125 ℃, the glycol content is 5.01 wt%, and the side-draw glycol is enriched and drawn.
The purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.95%, the recovery rate is 99.84%, the purity of the extractant at the bottom of the separation tower is 98.05%, and the loss of the extractant is 1.00%.
[ example 7 ]
According to the process flow diagram shown in FIG. 1, the extraction agent is n-octane, the ratio of the extraction agent to 1, 2-butylene oxide in the stream containing 1, 2-butylene oxide, the extraction agent and glycol is 10:1 by weight percent, the number of theoretical plates in the separation column is 15, and the 1 st theoretical plate above the reboiler return port is taken out from the side line of the separation column. The operating pressure of the separation tower is 0.12MPaA, the temperature is 73 ℃, the azeotropic temperature of the side-draw azeotrope is 135 ℃, the glycol content is 5.93 wt%, and the side-draw glycol is enriched and drawn.
The purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.95%, the recovery rate is 99.86%, the purity of the extractant at the bottom of the separation tower is 98.05%, and the loss of the extractant is 0.89%.
[ example 8 ]
According to the process flow diagram shown in FIG. 1, the extractant is n-octane, the ratio of the extractant to 1, 2-butylene oxide is 10:1 in weight percent in the material flow containing 1, 2-butylene oxide, the number of theoretical plates in the separation column is 45, and the 3 rd theoretical plate on the reboiler return opening is extracted from the side line of the separation column. The operating pressure of the separation tower is 0.13MPaA, the temperature is 76 ℃, the azeotropic temperature of the side-draw azeotrope is 137.5 ℃, the diol content is 6.16 wt%, and the side-draw diol is enriched and drawn.
The purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.95%, the recovery rate is 99.87%, the purity of the extractant at the bottom of the separation tower is 98.56%, and the loss of the extractant is 0.86%.
[ example 9 ]
According to the process flow diagram shown in FIG. 1, the extracting agent is n-octane, the ratio of the extracting agent to the 1, 2-butylene oxide in the material flow containing the 1, 2-butylene oxide, the extracting agent and the glycol is 10:1 in percentage by weight, the theoretical plate number of the separation tower is 60, and the 4 th theoretical plate on the reboiler return opening is extracted from the side line of the separation tower. The operating pressure of the separation tower is 0.15MPaA, the temperature is 77 ℃, the azeotropic temperature of the side-draw azeotrope is 138 ℃, the glycol content is 6.21 wt%, and the side-draw glycol is enriched and drawn.
The purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.95%, the recovery rate is 99.86%, the purity of the extractant at the bottom of the separation tower is 98.58%, and the loss of the extractant is 0.84%.
[ example 10 ]
According to the process flow diagram shown in FIG. 1, the extractant is n-octane, the ratio of the extractant to 1, 2-butylene oxide is 10:1 in weight percent in the material flow containing 1, 2-butylene oxide, the number of theoretical plates in the separation column is 80, and the side line of the separation column is extracted from the 6 th theoretical plate above the reboiler return port. The operating pressure of the separation tower is 0.17MPaA, the temperature is 80 ℃, the azeotropic temperature of the side-draw azeotrope is 142 ℃, the glycol content is 6.60 wt%, and the side-draw glycol is enriched and drawn.
The purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.95%, the recovery rate is 99.82%, the purity of the extractant at the bottom of the separation tower is 98.60%, and the loss of the extractant is 0.80%.
[ COMPARATIVE EXAMPLE 1 ]
According to the process flow diagram shown in FIG. 2, the extractant is n-octane, the ratio of the extractant to the 1, 2-butylene oxide is 12:1 in weight percent in the material flow containing the 1, 2-butylene oxide, the extractant and the glycol, and the theoretical plate number of the separation tower is 30.
In the case of ensuring the same purity and recovery of 1, 2-epoxybutane as in [ example 1 ], the diol concentration in the sidedraw stream was 5 times higher than that in the effluent extractant stream from the column bottom, i.e., the amount of extractant lost was 5 times higher than that in [ example 1 ] in the case of the same amount of impurities discharged, compared to [ example 1 ].
Claims (14)
1. A process for producing butylene oxide, comprising the step of separating a stream containing butylene oxide, an extractant and a glycol in a separation column;
the separation column is operated under conditions sufficient for the extractant and the diol to form an azeotrope, and
withdrawing a stream comprising an extractant and a glycol azeotrope in the separation column sidedraw;
the extractant is selected from C8A mixture of linear and branched alkanes.
2. The method of claim 1, wherein the conditions sufficient for the extractant and the glycol to form an azeotrope comprise: the pressure is 0.02-0.40 MPaA, and the temperature of the azeotrope is 80-180 ℃.
3. The method of claim 2, wherein the conditions sufficient for the extractant and the diol to form an azeotrope comprise: the pressure is 0.10-0.20 MPaA, and the temperature of the azeotrope is 120-150 ℃.
4. The process for producing butylene oxide according to claim 1, wherein the number of theoretical plates of the separation column is 15 to 80.
5. The process for producing butylene oxide according to claim 4, wherein the number of theoretical plates of the separation column is 20 to 65.
6. The process for producing butylene oxide according to claim 5, wherein the number of theoretical plates of the separation column is 20 to 50.
7. The method for producing butylene oxide according to claim 1, wherein the azeotrope is extracted from the side of the separation column at a position 1 to 8 theoretical plates above a reboiler return port at the bottom of the separation column.
8. A process for producing butylene oxide according to claim 7, wherein the azeotrope is withdrawn from the side of the separation column at a position 2 to 6 theoretical plates above a reboiler outlet at the bottom of the separation column.
9. The method for producing butylene oxide according to claim 8, wherein the azeotrope is extracted from the side of the separation column at a position 2 to 4 theoretical plates above a reboiler return opening at the bottom of the separation column.
10. The method for producing butylene oxide according to claim 1, wherein the ratio of the extractant to butylene oxide in the stream containing butylene oxide, the extractant and the glycol is (2-25): 1 in percentage by weight.
11. The method for producing butylene oxide according to claim 10, wherein the ratio of the extractant to butylene oxide in the stream containing butylene oxide, the extractant and the glycol is (3-20): 1 in percentage by weight.
12. The method for producing butylene oxide according to claim 11, wherein the ratio of the extractant to butylene oxide in the stream containing butylene oxide, the extractant and the glycol is (5-13): 1 in percentage by weight.
13. The process for producing butylene oxide according to claim 1, wherein the stream containing butylene oxide, the extractant and the glycol is derived from an extract product stream obtained by extractive distillation of an olefin epoxidation reaction product.
14. The process for producing butylene oxide according to claim 1, wherein the diol comprises a hydrolysate of butylene oxide and/or an isomer thereof.
Priority Applications (19)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711241136.1A CN109851587B (en) | 2017-11-30 | 2017-11-30 | Method for producing butylene oxide |
| SG11202005095WA SG11202005095WA (en) | 2017-11-30 | 2018-11-30 | Method and system for producing epoxyalkane |
| JP2020529524A JP7066849B2 (en) | 2017-11-30 | 2018-11-30 | Production method and system of alkylene oxide |
| PT188844237T PT3719008T (en) | 2017-11-30 | 2018-11-30 | Alkylene oxide production method and production system |
| SG11202005098UA SG11202005098UA (en) | 2017-11-30 | 2018-11-30 | Method and system for producing epoxyalkane |
| EP18883987.2A EP3719009A4 (en) | 2017-11-30 | 2018-11-30 | Method and system for producing epoxyalkane |
| KR1020207018147A KR102532058B1 (en) | 2017-11-30 | 2018-11-30 | Alkylene oxide production method and production system |
| EP18884423.7A EP3719008B1 (en) | 2017-11-30 | 2018-11-30 | Alkylene oxide production method and production system |
| KR1020207018148A KR102458887B1 (en) | 2017-11-30 | 2018-11-30 | Method and system for production of alkylene oxide |
| RU2020121678A RU2746482C1 (en) | 2017-11-30 | 2018-11-30 | Method and system for producing epoxyalkane |
| PCT/CN2018/118506 WO2019105451A1 (en) | 2017-11-30 | 2018-11-30 | Alkylene oxide production method and production system |
| BR112020010893-6A BR112020010893B1 (en) | 2017-11-30 | 2018-11-30 | METHOD FOR PRODUCING EPOXYALKANE |
| RU2020121556A RU2760003C1 (en) | 2017-11-30 | 2018-11-30 | Method and system for synthesising alkylene oxide |
| PCT/CN2018/118519 WO2019105453A1 (en) | 2017-11-30 | 2018-11-30 | Method and system for producing epoxyalkane |
| US16/768,663 US11773072B2 (en) | 2017-11-30 | 2018-11-30 | Method and system for producing epoxyalkane |
| US16/768,662 US11591303B2 (en) | 2017-11-30 | 2018-11-30 | Method and system for producing epoxyalkane |
| JP2020529567A JP7185691B2 (en) | 2017-11-30 | 2018-11-30 | Alkylene oxide production method and production system |
| BR112020010871-5A BR112020010871A2 (en) | 2017-11-30 | 2018-11-30 | method and system for the production of epoxyalkane |
| ES18884423T ES2942000T3 (en) | 2017-11-30 | 2018-11-30 | Production method and production system of alkylene oxide |
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