Device for preparing 1-butene from etherified C4

Abstract

The utility model relates to the technical field of petrochemical engineering, in particular to a device for preparing 1-butene from etherified C4. The device for preparing 1-butene from etherified C4 comprises an alkane-alkene separation unit, a selective hydrogenation reactor, a deep etherification reactor and a precise rectification unit which are sequentially arranged along a material flow direction, and also comprises a methanol recovery unit, and the methanol recovery unit is connected with the precise rectification unit and the deep etherification reactor. According to the utility model, the olefin content is concentrated in an alkane-olefin separation manner; under the condition of higher olefin content, the 1-butene is easier to separate, and the loss of the 1-butene is smaller; 1-butene product separation and methanol recovery are carried out after deep etherification, on one hand, methanol is enriched during 1-butene separation and enters the top of the light component removal tower, so that the amount of C4 needing to be treated for methanol recovery can be reduced, the concentration of methanol is increased, and the energy consumption of methanol recovery is reduced; on the other hand, the problem that the water content of the 1-butene product exceeds the standard is avoided.

Description

TECHNICAL FIELD

[0001] The utility model relates to the technical field of petroleum chemical industry, concretely relates to the device of 1-butene of ether post carbon four. BACKGROUND

[0002] Butene is carbon four olefin, can be used as polyethylene comonomer, also can be used for producing methyl ethyl ketone, amyl aldehyde, isodecyl alcohol and other fine chemical products, the use is very extensive.1-Butene mostly comes from carbon four hydrocarbon, is mainly separated through super-precision rectification or extraction rectification.Using the byproduct mixed carbon four of steam cracking device to produce 1-butene method is to extract mixed carbon four of steam cracking device through butadiene, then converts isobutene through MTBE device and takes as 1-butene device's feed, removes light component and water through the isobutene removal tower, then separates through 1-butene rectification tower and obtains polymerization grade 1-butene.Mixed carbon four separation is the main process route of producing 1-butene, and domestic numerous oil refineries, catalytic cracking device, ethylene cracking device, coal methanol to olefin device can provide abundant mixed carbon four raw materials. Because the relative volatility of each component of mixed carbon four is close, it is difficult to separate through ordinary rectification method. From the angle of saving energy consumption, reducing process complexity, needs to remove butadiene, isobutene and other components in mixed carbon four in advance, so that 1-butene is easy to separate and purify. The general practice is to realize the separation or conversion of butadiene through butadiene extraction, selective hydrogenation and other technologies on the basis of mixed carbon four separation process technology, then optimizes the conversion and separation of isobutene through etherification, and finally obtains 1-butene through precision rectification. This process has limited raw material sources, and with the increasing demand for 1-butene, it is necessary to expand the raw material sources of 1-butene, and there are many catalytic cracking devices and coal to olefin devices, in the process of 1-butene separation, butadiene and isobutene have similar boiling points with 1-butene, so the above two components must be removed to obtain 1-butene product, and then 1-butene product is obtained through precision rectification.

[0003] The ether post carbon four compound refers to the carbon four fraction treated through etherification reaction in the oil refining process. Compared with mixed carbon four, most of the olefins in the treated carbon four fraction have been converted into ethers, so the olefin content in the ether post carbon four fraction is low, mainly including butane, unreacted butene and other saturated hydrocarbons. Because the olefin content in the ether post carbon four is low, the process for preparing 1-butene from this raw material needs a lot of energy consumption, and 1-butene is difficult to separate and has large loss.

[0004] The patent CN212864604U discloses a device and process for preparing 1-butene by using C4 fraction, which is especially suitable for carbon four raw materials rich in n-butane, and the device comprises a selective hydrogenation unit, an etherification unit and a precision rectification unit arranged in sequence along the material flow direction, further comprises an extraction pre-fractionation unit, wherein the extraction pre-fractionation unit is arranged between the selective hydrogenation unit and the etherification unit, or is connected after the precision rectification unit, and a 2-butene isomerization unit is further connected after the extraction pre-fractionation unit. Utility model content

[0005] The utility model discloses to solve the problem of 1-butene energy consumption of ether after carbon four production, product separation is difficult, provide a device for 1-butene of ether after carbon four.

[0006] In order to solve the above problem, the technical scheme of the utility model is:

[0007] The device for 1-butene of ether after carbon four, including the alkyl olefin separation unit, the selective hydrogenation reactor, the depth etherification reactor, the precision rectification unit that alkyl olefin separation unit, selective hydrogenation reactor, depth etherification reactor are arranged in sequence along the material flow direction, still include the recovery methanol unit, the recovery methanol unit is connected precision rectification unit and depth etherification reactor.

[0008] The utility model first enriches olefin content through the mode of alkyl olefin separation.Under the condition of higher olefin content, it is easier to separate 1-butene, and the loss of 1-butene is smaller.

[0009] Further, the alkyl olefin separation unit is connected with the selective hydrogenation reactor through a hydrogenation feed pipe, the selective hydrogenation reactor is connected with the depth etherification reactor through an etherification feed pipe, the depth etherification reactor is connected with the precision rectification unit through a light removal feed pipe, and the selective hydrogenation reactor is connected with a hydrogen pipeline.

[0010] Further, the alkyl olefin separation unit comprises an alkyl olefin extraction separation tower and a solvent recovery tower arranged in sequence along the material flow direction.

[0011] Further, the alkyl olefin extraction separation tower is provided with a raw material feed pipe, the top of the alkyl olefin extraction separation tower is provided with an alkane separation pipe, the bottom is connected with the solvent recovery tower through a solvent transportation pipe, and the bottom of the solvent recovery tower is connected with the feed inlet of the alkyl olefin extraction separation tower through a solvent recovery pipe.

[0012] Further, the precision rectification unit comprises a light removal tower, a heavy removal tower and a heavy component separation tower arranged in sequence along the material flow direction.

[0013] Further, the bottom of the light-removing column is connected with a heavy-removing column through a heavy-removing feeding pipe, the heavy-removing column is connected with a heavy component separation column through a heavy component conveying pipe, the top of the heavy-removing column is connected with a 1-butene conveying pipe, the top of the heavy component separation column is connected with a column top discharging pipe, and the bottom is connected with a column bottom discharging pipe.

[0014] Further, the methanol recovery unit comprises a methanol extraction column and a methanol recovery column arranged in sequence along the material flow direction, the top of the light-removing column is connected with the methanol extraction column through a light component conveying pipe, the bottom of the methanol recovery column is connected with the feeding port of the methanol extraction column through a column bottom water circulating pipe, the top of the methanol recovery column is connected with a mixer in parallel with a fresh methanol feeding pipe through a methanol recovery pipe, and the mixer is connected with the feeding port of a deep etherification reactor through a mixed methanol feeding pipe.

[0015] The 1-butene product is separated first after deep etherification, and then the methanol recovery process is carried out, on the one hand, the methanol is enriched during the 1-butene separation, the methanol enters the top of the light-removing column, the amount of carbon four that needs to be treated for methanol recovery is reduced, the concentration of methanol is improved, and the energy consumption of methanol recovery is reduced, on the other hand, water is used as an extractant in the methanol recovery process, therefore, if the methanol recovery is carried out before the 1-butene product is separated, the water content of the 1-butene may exceed the standard, and the acid substances brought by deep etherification will cause the dehydration package of the reflux tank at the top of the light-removing column to be severely corroded.

[0016] Further, the methanol extraction column is connected with the methanol recovery column through a rich liquid conveying pipe, and the top of the methanol extraction column is connected with an isobutane conveying pipe.

[0017] Working principle: the raw material ether after carbon four in the utility model first passes through the alkyl olefin extraction separation column, extracts olefin through a solvent, discharges and separates most of the alkane from an alkane separation pipe, enriches 1-butene to reduce the energy consumption of subsequent separation, carries the solvent with olefin into the solvent recovery column, desorbs and discharges the olefin, and then the regenerated solvent is transported to the alkyl olefin extraction separation column through a solvent recovery pipe for recycling, the desorbed olefin is converted into butadiene through a selective hydrogenation reactor, then is mixed with methanol and enters a deep etherification reactor for etherification reaction, converts isobutene therein, and then enters the light-removing column and the heavy-removing column for separation, the bottom product of the light-removing column enters the heavy-removing column for separation, the top obtains 1-butene product, the bottom enters the heavy component separation column for separation, the top obtains n-butane and 2-butene, and the column bottom is methyl tertiary butyl ether, methyl secondary butyl ether and tertiary butanol.

[0018] The isobutane and methanol at the top of the light removal column enter a methanol extraction column, and are extracted and separated with water at the bottom of the methanol recovery column in the methanol extraction column, light components such as isobutane are obtained at the top of the methanol extraction column, and the water containing methanol at the bottom of the methanol extraction column enters the methanol recovery column to recover methanol, the recovered methanol is transported through a methanol recovery pipe, mixed with fresh methanol in a mixer in a mixed methanol feeding pipe, and then transported to the deep etherification reactor as raw material. The extraction water at the bottom of the methanol recovery column is recycled.

[0019] The beneficial effects of the utility model are as follows:

[0020] (1) The utility model separates alkyl and olefin first, enriches olefin, the boiling point of isobutene and 1-butene is similar, and the content of 1-butene in carbon four after etherification is low. The higher the concentration of 1-butene is, the more the loss of 1-butene can be reduced due to the existence of isobutene, and the amount of material for subsequent separation can also be reduced, the reflux is reduced, and the energy consumption is greatly saved, so the content of olefin is enriched by the mode of alkyl and olefin separation first. Under the condition of high olefin content, 1-butene is easy to separate, and the loss of 1-butene is small.

[0021] (2) The utility model separates 1-butene product first after deep etherification, and then carries out the methanol recovery process. On the one hand, methanol is enriched in the separation of 1-butene, methanol enters the top of the light removal column, the amount of carbon four that needs to be treated for methanol recovery is reduced, the concentration of methanol is improved, and the energy consumption of methanol recovery is reduced. On the other hand, water is used as an extractant in the methanol recovery process, so if the methanol recovery is carried out before the separation of 1-butene product, the water content of 1-butene may exceed the standard, and the acid substances brought by deep etherification will cause the dehydration package of the reflux tank at the top of the light removal column to be seriously corroded. BRIEF DESCRIPTION OF DRAWINGS

[0022] The drawings described herein are used to provide further understanding of the utility model and constitute a part of the utility model. The illustrative embodiments of the utility model and the description thereof are used to explain the utility model, and do not constitute improper limitation on the utility model. In the drawings:

[0023] Figure 1 It is a structure schematic view of the device for preparing 1-butene from carbon four after etherification of the utility model;

[0024] In the drawings:

[0025] 1, select hydrogenation reactor; 2, depth etherification reactor; 3, light column; 4, heavy column; 5, methanol extraction column; 6, methanol recovery column; 7, heavy component separation column; 8, hydrogenation feed pipe; 9, etherification feed pipe; 10, light feed pipe; 11, heavy feed pipe; 12, heavy component transport pipe; 13, fresh methanol feed pipe; 14, mixer; 15, methanol recovery pipe; 16, mixed methanol feed pipe; 17, light component transport pipe; 18, 1-butene transport pipe; 19, rich liquid transport pipe; 20, bottom water circulation pipe; 21, isobutane transport pipe; 22, separation column top discharge pipe; 23, separation column bottom discharge pipe; 24, alkyl olefin extraction separation column; 25, solvent recovery column; 26, raw material feed pipe; 27, solvent transport pipe; 28, alkane separation pipe; 29, solvent recovery pipe; 30, hydrogen pipeline. DETAILED DESCRIPTION

[0026] The utility model can be understood in the following combining with the embodiment.

[0027] In the description of the utility model, it needs to be understood that the orientation or position relationship indicated by the terms "center", "longitudinal", "transverse", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer" and the like is based on the orientation or position relationship shown in the drawings, and is only for the convenience of describing the utility model and simplifying the description, and therefore cannot be understood as indicating or implying that the indicated device or element must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the utility model. In addition, the terms "first", "second" and the like are only for the purpose of description, and cannot be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features limited by "first", "second" and the like can be explicitly or implicitly included one or more. In the description of the utility model, the meaning of "a plurality of" is two or more, unless otherwise specified.

[0028] In the description of the utility model, it needs to be explained that, unless otherwise explicitly specified and limited, the terms "mounting", "connection", "connection" should be understood broadly, for example, it can be fixedly connected, or it can be detachably connected, or integrally connected; it can be mechanically connected, or it can be electrically connected; it can be directly connected, or it can be indirectly connected through an intermediate medium, or it can be the communication between two elements. For ordinary skilled in the art, the specific meaning of the above terms in the utility model can be understood through specific circumstances.

[0029] In one embodiment, as Figure 1As shown, the device for preparing 1-butene from etherized C4, comprising an alkyl-alkene separation unit, a selective hydrogenation reactor 1, a deep etherification reactor 2, a precision rectification unit arranged in sequence along the material flow direction, and a methanol recovery unit connected with the precision rectification unit and the deep etherification reactor 2.

[0030] The alkyl-alkene separation unit is used to enrich the content of olefins.

[0031] The alkyl-alkene separation unit is connected with the selective hydrogenation reactor 1 through a hydrogenation feed pipe 8, the selective hydrogenation reactor 1 is connected with the deep etherification reactor 2 through an etherification feed pipe 9, the deep etherification reactor 2 is connected with the precision rectification unit through a light component removal feed pipe 10, and the selective hydrogenation reactor 1 is connected with a hydrogen pipeline 30.

[0032] The alkyl-alkene separation unit comprises an alkyl-alkene extraction separation tower 24 and a solvent recovery tower 25 arranged in sequence along the material flow direction.

[0033] The alkyl-alkene extraction separation tower 24 is provided with a raw material feed pipe 26, an alkane separation pipe 28 is arranged at the top of the alkyl-alkene extraction separation tower 24, a solvent transportation pipe 27 is arranged at the bottom of the alkyl-alkene extraction separation tower 24 and connected with the solvent recovery tower 25, and a solvent recovery pipe 29 is arranged at the bottom of the solvent recovery tower 25 and connected with the feed inlet of the alkyl-alkene extraction separation tower 24.

[0034] The precision rectification unit comprises a light component removal tower 3, a heavy component removal tower 4 and a heavy component separation tower 7 arranged in sequence along the material flow direction.

[0035] The light component removal tower 3 is connected with the heavy component removal tower 4 through a heavy component removal feed pipe 11, the heavy component removal tower 4 is connected with the heavy component separation tower 7 through a heavy component transportation pipe 12, a 1-butene transportation pipe 18 is arranged at the top of the heavy component removal tower 4, a separation tower top discharge pipe 22 is arranged at the top of the heavy component separation tower 7, and a separation tower bottom discharge pipe 23 is arranged at the bottom of the heavy component separation tower 7.

[0036] The methanol recovery unit comprises a methanol extraction tower 5 and a methanol recovery tower 6 arranged in sequence along the material flow direction, the light component removal tower 3 is connected with the methanol extraction tower 5 through a light component transportation pipe 17, the methanol recovery tower 6 is connected with the feed inlet of the methanol extraction tower 5 through a tower bottom water circulation pipe 20, the methanol recovery tower 6 is connected with a mixer 14 in parallel with a fresh methanol feed pipe 13 through a methanol recovery pipe 15, and the mixer 14 is connected with the feed inlet of the deep etherification reactor 2 through a mixed methanol feed pipe 16.

[0037] The utility model discloses depth etherization is carried out 1-butene product separation first, and then methanol recovery process is carried out, one aspect is because methanol is enriched when 1-butene separation, and methanol enters the top of light removal column 3, can reduce the carbon four amount that methanol recovery needs to handle, improves the concentration of methanol, reduces the energy consumption of methanol recovery, the other aspect is that methanol recovery process needs to use water as extractant, therefore if methanol recovery is carried out before 1-butene product separation, can cause 1-butene water content to exceed the standard, and the acid material from depth etherization can cause the serious corrosion of the dehydration package of the reflux tank in the top of light removal column in water.

[0038] It can be understood that the methanol extraction column 5 is connected with the methanol recovery column 6 through the rich liquid conveying pipe 19, and the top of the methanol extraction column 5 is connected with the isobutane conveying pipe 21.

[0039] Working principle: the raw material ether after carbon four of the utility model discloses first through alkyl olefin extraction separation tower 24 through solvent olefin extraction, most of alkane is discharged from alkane separation pipe 28 and separated, 1-butene is enriched and the follow-up separation energy consumption is reduced, the solvent carrying olefin enters solvent recovery column 25, and the olefin is desorbed and exported, and the regenerated solvent is transported to alkyl olefin extraction separation tower 24 through solvent recovery pipe 29 and is recycled, the desorbed olefin is converted into butadiene through the selection hydrogenation reactor 1, then is mixed with methanol and enters depth etherification reactor 2 to carry out etherification reaction, and the isobutene in the depth etherification reactor 2 is converted into. Then enter light removal column 3 and heavy removal column 4 and separate, the bottom product of light removal column 3 enters heavy removal column 4 and separates, the top obtains 1-butene product, the bottom enters heavy component separation column 7 and separates, the top obtains n-butane and 2-butene, and the bottom is methyl tertiary butyl ether, methyl sec-butyl ether tertiary butanol and the like.

[0040] The isobutane and methanol in the top of the light removal column 3 enter the methanol extraction column 5, and the water in the bottom of the methanol recovery column 6 is extracted and separated in the methanol extraction column 5, the light components such as isobutane are obtained in the top of the methanol extraction column 5, the water containing methanol in the bottom of the methanol extraction column 5 enters the methanol recovery column 6 to recover methanol, the recovered methanol is transported through the methanol recovery pipe 15, mixed with fresh methanol in the fresh methanol feeding pipe 13 in the mixer 14, and then transported to the depth etherification reactor 2 through the mixed methanol feeding pipe 16 and used as raw material. The extraction water in the bottom of the methanol recovery column 6 is recycled.

[0041] The above only is the embodiment of the utility model, and does not limit the utility model. For those skilled in the art, the utility model can have various changes and changes. Any modification, equivalent replacement, improvement and the like within the spirit and principle of the utility model should be included in the claim range of the utility model.

Claims

1. An apparatus for producing 1-butene from etherate C4s, characterized by, The alkylene separation unit, the selective hydrogenation reactor (1), the deep etherification reactor (2), the precise rectification unit are arranged in sequence along the material flow direction, and the recovery methanol unit is further arranged.

2. The apparatus for producing 1-butene from etherate C4 according to claim 1, characterized in that, The alkylene separation unit is connected with the selective hydrogenation reactor (1) through a hydrogenation feed pipe (8), the selective hydrogenation reactor (1) is connected with the deep etherification reactor (2) through an etherification feed pipe (9), the deep etherification reactor (2) is connected with the precise rectification unit through a light component removal feed pipe (10), and the selective hydrogenation reactor (1) is connected with a hydrogen pipeline (30).

3. The apparatus for making 1-butene from etherate C4 according to claim 1, characterized in that, The alkylene separation unit comprises an alkylene extraction separation tower (24) and a solvent recovery tower (25) arranged in sequence along the material flow direction.

4. The apparatus for producing 1-butene from etherate C4 according to claim 3, characterized in that, The alkylene extraction separation tower (24) is provided with a raw material feed pipe (26), the alkylene extraction separation tower (24) is provided with an alkane separation pipe (28) at the top and is connected with the solvent recovery tower (25) through a solvent transportation pipe (27) at the bottom, and the solvent recovery tower (25) is connected with the alkylene extraction separation tower (24) through a solvent recovery pipe (29) at the bottom.

5. The apparatus for making 1-butene from etherate C4 according to claim 1, characterized in that, The precise rectification unit comprises a light component removal tower (3), a heavy component removal tower (4) and a heavy component separation tower (7) arranged in sequence along the material flow direction.

6. The apparatus for making 1-butene from etherate C4 according to claim 5, characterized in that, The light component removal tower (3) is connected with the heavy component removal tower (4) through a heavy component removal feed pipe (11) at the bottom, the heavy component removal tower (4) is connected with the heavy component separation tower (7) through a heavy component transportation pipe (12), the heavy component removal tower (4) is connected with a 1-butene transportation pipe (18) at the top, the heavy component separation tower (7) is connected with a separation tower top discharge pipe (22) at the top and is connected with a separation tower bottom discharge pipe (23) at the bottom.

7. The apparatus for making 1-butene from etherate C4 according to claim 5, characterized in that, The recovery methanol unit comprises a methanol extraction tower (5) and a methanol recovery tower (6) arranged in sequence along the material flow direction, the light component removal tower (3) is connected with the methanol extraction tower (5) through a light component transportation pipe (17) at the top, the methanol recovery tower (6) is connected with the methanol extraction tower (5) through a bottom water circulation pipe (20) at the bottom, the methanol recovery tower (6) is connected with a mixer (14) through a methanol recovery pipe (15) in parallel with a fresh methanol feed pipe (13) at the top, and the mixer (14) is connected with the deep etherification reactor (2) through a mixed methanol feed pipe (16) at the feed port.

8. The apparatus for ether after C4 to make 1-butene of claim 7, characterized in that, The methanol extraction tower (5) is connected with the methanol recovery tower (6) through a rich liquid transportation pipe (19), and the methanol extraction tower (5) is connected with an isobutane transportation pipe (21) at the top.

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