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CN119186000A - Method for reversing and driving MTBE-butene device - Google Patents

Method for reversing and driving MTBE-butene device Download PDF

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Publication number
CN119186000A
CN119186000A CN202411326508.0A CN202411326508A CN119186000A CN 119186000 A CN119186000 A CN 119186000A CN 202411326508 A CN202411326508 A CN 202411326508A CN 119186000 A CN119186000 A CN 119186000A
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tower
butene
heavy
mtbe
carbon
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薛媛媛
孙振江
张伟
王飞虎
杨传贺
张乐乐
祁兴
许晓阳
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Pucheng Clean Energy Chemical Co Ltd
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Pucheng Clean Energy Chemical Co Ltd
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Priority to CN202411326508.0A priority Critical patent/CN119186000A/en
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/16—Fractionating columns in which vapour bubbles through liquid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/42—Regulation; Control
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/04—Purification; Separation; Use of additives by distillation
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The invention provides a method for reverse start-up of an MTBE-butene device, which belongs to the technical field of 1-butene preparation process, wherein heavy carbon in a mixed carbon four-tank is introduced into a first rectifying tower through a pipeline to remove light components, carbon four-distillation at the bottom of the first rectifying tower is distributed to a second rectifying tower, carbon four-distillation is separated in the second rectifying tower, heavy components are removed, part of gas at the top of the second rectifying tower is condensed by a condenser, and part of gas is sent out as butene-1 products, and n-butane and butene-2 at the bottom of the second rectifying tower are sent to an isomerization unit. The method can shorten the time for producing the qualified products of the 1-butene from 72 hours to 24 hours, effectively shortens the time for producing the 1-butene and improves the preparation efficiency.

Description

Method for reversing and driving MTBE-butene device
Technical Field
The invention belongs to the technical field of 1-butene preparation processes, and particularly relates to a method for turning on an MTBE-butene device.
Background
Polymerization grade 1-butene can be produced by dimerization of ethylene, and since ethylene itself is expensive, the production cost is high, and it cannot be applied industrially on a large scale. And the mixed carbon four produced in the petroleum hydrocarbon cracking process is an excellent raw material for producing high-purity 1-butene after the 1, 3-butadiene is removed by extraction. Therefore, how to extract 1-butene from mixed carbon four is a hot spot problem of research. The main components of the mixed carbon four are isobutane, n-butane, isobutene, 1-butene, trans-2-butene, cis-2-butene and1, 3-butadiene, wherein the boiling points of the three components of the 1-butene, the isobutene and the 1, 3-butadiene are very close, so that the extracted carbon four is directly used as a raw material, high-purity 1-butene cannot be obtained by adopting a separation method, and the isobutene and the 1, 3-butadiene must be removed to very low content.
At present, methyl tertiary butyl ether is separated from mixed carbon four after MTBE etherification in industry, then isobutene and 1, 3-butadiene in the residual materials are removed after catalytic selective hydrogenation, the main components after the catalytic hydrogenation are H 2、H2 O, methanol, isobutane, 1-butene, n-butane, trans-2-butene and cis-2-butene, and then the high-purity 1-butene is obtained through rectification of a first rectifying tower and a second rectifying tower, and a heavy four-carbon product is produced by a mixed carbon four-tank connected with the bottom of the second rectifying tower. However, in the process, the mixed carbon four raw materials can be started after waiting for the DMTO and olefin separation device to start to stably produce qualified mixed carbon four, and the 1-butene is refined, so that the time for preparing the 1-butene is longer, and the production efficiency is influenced.
Accordingly, it is desirable to provide a process capable of shortening the 1-butene production time.
Disclosure of Invention
The invention provides a method for reversing and starting an MTBE-butene device, which aims to solve the problem that in the prior art, 1-butene can be refined only after mixed four-carbon production is stable, so that the preparation efficiency of 1-butene is low.
In order to achieve the above object, the technical scheme of the present invention is as follows.
An MTBE-butene unit reverse driving method comprises the following steps:
introducing heavy tetracarbon in the mixed carbon tetracarbon tank into a first rectifying tower through a pipeline to remove light components, distributing carbon tetracarbon fraction at the bottom of the first rectifying tower into a second rectifying tower, separating the carbon tetracarbon fraction in the second rectifying tower, removing heavy components, condensing part of gas at the top of the second rectifying tower through a condenser, and delivering part of gas as butane 1-ene products, and delivering n-butane and 2-butene at the bottom of the second rectifying tower into an isomerization unit;
And after the qualified mixed carbon four is produced by the DMTO and olefin separation device, replacing the heavy carbon four with the mixed carbon four, and introducing the mixed carbon four into the first rectifying tower through a pipeline, and then starting the whole system.
In another preferred embodiment, the first rectification column comprises an upper column and a lower column;
The gas phase material of the lower tower enters the bottom of the upper tower through a pipeline to be used as ascending gas phase material flow, and the liquid of the upper tower is pumped to the top of the lower tower through a middle pump to be used as internal reflux;
the bottom material of the lower tower is carbon four fraction from which isobutane light components are removed, and is pumped out by a bottom pump and sent to a second rectifying tower.
In another preferred embodiment, the second rectification column comprises an upper stage column and a lower stage column;
The gas at the top of the upper tower enters a tower top reflux tank after being condensed by a condenser, and is pressurized by a reflux pump, wherein a part of the gas is fed into the tower top of the upper tower as reflux, and a part of the gas is fed out as 1-butene product;
the gas phase material at the top of the lower tower enters the bottom of the upper tower through a pipeline to be used as ascending gas phase material flow, the liquid at the bottom of the upper tower is pumped to the top of the lower tower through a middle pump to be used as internal reflux, the heavy fraction mainly comprising n-butane and butene-2 is produced at the bottom of the lower tower, pumped out through a tower bottom pump, sent into a butene-2 cooler to be cooled, one part of the heavy fraction is sent into an isomerization unit to be used as raw material, and the other part of the heavy fraction is sent out after being mixed with heavy carbon four returned by the isomerization unit as a byproduct.
In another preferred embodiment, the lower column of the first rectification column is in communication with the upper section of the second rectification column via a pipeline.
In another preferred embodiment, the pressure range of the first rectifying tower is 0.55-0.75 MPa, the tower top temperature is 45-55 ℃, the tower bottom temperature is 65-80 ℃, and the tower top reflux ratio is 1320.
In another preferred embodiment, the pressure range of the second rectifying tower is 0.40-0.50 MPa, the tower top temperature is 40-55 ℃, the tower bottom temperature is 55-70 ℃, and the tower top reflux ratio is 28.
In another preferred embodiment, the heavy four carbon specific source process in the mixed carbon four tank is as follows:
and extracting heavy carbon four from the tower bottom of the second rectifying tower in two ways, wherein one way is used as the feeding of the isomerization unit, and the other way is used as a heavy carbon four product to be sent to a mixed carbon four tank.
In another preferred embodiment, the heavy tetracarbons include n-butane, cis-2-butene, trans-2-butene, and butene.
In another preferred embodiment, after the DMTO and olefin separation device produces acceptable mixed carbon four, heavy carbon four is replaced with mixed carbon four and introduced into the first rectifying tower through a pipeline, and full system start-up is performed.
Compared with the prior art, the invention has the following beneficial effects:
According to the invention, the heavy four carbon in the production line is directly introduced into the 1-butene rectifying tower for directly producing 1-butene, so that the time for producing 1-butene is effectively prolonged. In the whole production process, the driving can be carried out without waiting for mixing four carbons, the driving time can be effectively shortened by reversing the driving, and the production efficiency is improved. And after the DMTO and olefin separation device produces qualified mixed carbon four, slowly cutting the feed from heavy carbon four to mixed carbon four for full-system start-up. Compared with the traditional preparation of qualified 1-butene products, the method provided by the invention requires only 24 hours, so that the production efficiency is effectively improved.
Drawings
FIG. 1 is a process for preparing 1-butene in a prior art MTBE-butene unit.
FIG. 2 is a process for preparing 1-butene by reverse driving in the embodiments of the present invention.
Detailed Description
The present invention will be described in further detail with reference to the following examples in order to make the objects, technical solutions and advantages of the present invention more apparent. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.
The experimental methods described in the examples below are conventional methods unless otherwise specified, and the reagents and materials described herein are commercially available.
At present, methyl tertiary butyl ether is separated from mixed carbon four after MTBE etherification in industry, then isobutene and1, 3-butadiene in the residual materials are removed after catalytic selective hydrogenation, the main components after the catalytic hydrogenation are H 2、H2 O, methanol, isobutane, 1-butene, n-butane, trans-2-butene and cis-2-butene, and then the high-purity 1-butene can be obtained through rectification.
The flow of the prior art for producing 1-butene is shown in fig. 1, and is the start-up sequence of a normal MTBE-butene device, after qualified mixed carbon four is produced by a DMTO and olefin separation device, the mixed carbon four is fed into a first rectifying tower T3001A/B through a pipeline for rectification, and light component water, propane, isobutane and the like are removed. The gas at the top of the tower enters a reflux tank V3001 after passing through a condenser E3001A/B, is pumped out by a reflux pump P3001A/B, part of the gas is pumped into the top of the tower to be used as reflux, and the other part of the gas is used as a light-carbon four-sending device rich in isobutane byproducts, and a small amount of non-condensable gas at the top of the tower is discharged into a torch through a regulating valve. Because the first rectifying tower is relatively high, the first rectifying tower needs to be divided into two sections, namely an upper section T3001A and a lower section T3001B. The gas phase material of the lower tower T3001B of the first rectifying tower enters the bottom of the upper tower T3001A through a pipeline to be used as ascending gas phase material flow, and the liquid of the tower kettle of the T3001A is sent to the top of the T3001B through an intermediate pump P3003A/B to be used as internal reflux. The tower bottom material of the T3001B is carbon four fraction from which light components such as isobutane are removed, and is pumped out by a tower bottom pump P3002A/B and sent to a second rectifying tower T3002A/B. The bottom of the first rectifying tower is heated by a reboiler E3002, and the heat source is the secondary low-pressure steam from the system. The materials from the first rectifying tower are separated in the second rectifying tower, and heavy components such as 2-butene, n-butane and the like are removed. The gas at the top of the upper tower T3002A of the second rectifying tower enters a tower top reflux tank V3002 after being condensed by a condenser E3003A/B, and is pressurized by a second rectifying tower top reflux pump P3004A/B, a part of the gas is fed into the upper tower top of the second rectifying tower as reflux, and the other part of the gas is used as a butene-1 product, the purity is more than or equal to 99 percent, and the gas is sent out of a boundary zone. The bottom of the second rectifying tower is heated by a reboiler E3004, and the heat source is the secondary low-pressure steam from the system.
The second rectifying column also has to be divided into two sections, respectively referred to as the upper section T3002A and the lower section T3002B. The gas phase material at the top of the T3002B enters the bottom of the T3002A as an ascending gas phase material flow, and the liquid in the tower bottom of the T3002A is sent to the top of the T3002B through an intermediate pump P3006A/B for internal reflux. The bottom material of T3002B is a heavy fraction mainly comprising n-butane and 2-butene, is pumped out by a bottom pump P3005A/B, is sent to a 2-butene cooler E3005 for cooling, and is sent to an isomerization unit as a raw material, and is sent out of the device after being mixed with heavy carbon four returned by the isomerization unit as a byproduct.
The heavy carbon four from the pump P3005A/B enters a feeding buffer tank V4001, the materials are gasified through an E4001, the gasified carbon four materials are further subjected to heat exchange with a reaction product in a feeding and discharging heat exchanger E4002 to about 286 ℃ and enter an electric heater EH4001, the raw materials are heated to the temperature required by the reaction to be 330 ℃, and then enter a reactor R4001 from the top to carry out isomerization reaction. The outlet gas of the reactor exchanges heat with the feed carbon four in a feed and discharge heat exchanger E4002, the temperature of the reaction gas after heat exchange is reduced to about 121 ℃, then the reaction gas enters a 1-butene concentration tower T4001, crude 1-butene product with the concentration of about 34% is obtained at the top of the tower, a circulating cooling water is adopted for condensation by a condenser E4003 at the top of the tower, after the liquid phase material of a reflux tank V4003 at the top of the tower is pressurized by a reflux pump P4001A/B of the 1-butene concentration tower, one part of the liquid phase material returns to the 1-butene concentration tower T4001 as reflux liquid, and the other part of the liquid phase material is sent to a lower tower T3001B of the first rectifying tower. The discharge of the tower bottom is mainly mixed carbon four fractions rich in 2-butene, and the materials are cooled by a tower bottom liquid cooler E4005 of the 1-butene concentration tower and then sent to a heavy carbon four product line.
According to the process, in the prior art, after qualified mixed carbon four is produced in a DMTO and olefin separation device, 1-butene can be separated and purified, and 1-butene is refined, so that the time for preparing 1-butene is long, and the production efficiency is influenced.
The process for preparing the 1-butene in the prior art can show that the raw material for preparing the 1-butene is mixed with the carbon four, the DMTO and the olefin separation device can be started after the qualified mixed carbon four is stably produced by starting, and the 1-butene is refined, so that the time for preparing the 1-butene is longer, and the production efficiency is influenced.
According to the invention, the heavy four-carbon components in the mixed carbon four-tank connected with the bottom of the second rectifying tower are utilized, the heavy four-carbon components are directly introduced into the first rectifying tower in a reverse driving mode, and 1-butene is separated and purified, so that the delicate efficiency of 1-butene is effectively improved, after the mixed four-carbon components are stably produced by the DMTO and olefin separating device, the introduction of the heavy four-carbon components at the bottom of the second rectifying tower into the first rectifying tower is stopped, and the produced mixed carbon four is introduced into the first rectifying tower, and the normal driving sequence is carried out. The method can effectively utilize the time of the DMTO and olefin separation device before qualified mixed carbon four is produced, improves the working efficiency, fully utilizes heavy four carbon components in the mixed carbon four tank connected with the bottom of the second rectifying tower, and effectively shortens the working time.
A method for driving an MTBE-butene plant upside down is described in detail below.
As shown in fig. 2, before the DMTO and olefin separation device does not produce qualified mixed carbon four, heavy carbon in the mixed carbon four tank connected with the lower section T3002B of the second rectifying tower is introduced into T3001A/B of the first rectifying tower through a pipeline for rectification, so as to remove light component water, propane, isobutane and the like. The gas at the top of the tower enters a reflux tank V3001 after passing through a condenser E3001A/B, is pumped out by a reflux pump P3001A/B, part of the gas is pumped into the top of the tower to be used as reflux, and the other part of the gas is used as a light-carbon four-sending device rich in isobutane byproducts, and a small amount of non-condensable gas at the top of the tower is discharged into a torch through a regulating valve.
Because the first rectifying tower is relatively high, the first rectifying tower needs to be divided into two sections, namely an upper section T3001A and a lower section T3001B. The gas phase material of the lower tower T3001B of the first rectifying tower enters the bottom of the upper tower T3001A through a pipeline to be used as ascending gas phase material flow, and the liquid of the tower kettle of the T3001A is sent to the top of the T3001B through an intermediate pump P3003A/B to be used as internal reflux. The tower bottom material of the lower section T3001B is carbon four fraction from which light components such as isobutane are removed, and is pumped out by a tower bottom pump P3002A/B and sent to a second rectifying tower T3002A/B. The bottom of the first rectifying tower is heated by a reboiler E3002, and the heat source is the secondary low-pressure steam from the system.
The materials from the first rectifying tower are separated in the second rectifying tower, and heavy components butene-2, n-butane and the like are removed. The gas at the top of the upper section tower T3002A of the second rectifying tower enters a tower top reflux tank V3002 after being condensed by a condenser E3003A/B, and is pressurized by a second rectifying tower top reflux pump P3004A/B, one part of the gas is fed into the upper tower top of the second rectifying tower as reflux, the other part of the gas is used as a butene-1 product, the purity is more than or equal to 99 percent, and the gas is sent out of a boundary zone. The bottom of the lower tower T3002B produces heavy fraction mainly comprising n-butane and 2-butene, the heavy fraction is pumped out by a tower bottom pump, and is sent to a 2-butene cooler for cooling, one part of the heavy fraction is sent to an isomerization unit to be used as a raw material, and the other part of the heavy fraction is sent out after being mixed with heavy carbon four returned by the isomerization unit as a byproduct.
And after the qualified mixed carbon four is produced by the DMTO and olefin separation device, replacing the heavy carbon four with the mixed carbon four, and introducing the mixed carbon four into the first rectifying tower through a pipeline, and then starting the whole system.
The time for obtaining qualified 1-butene products is 24 hours, and the time for producing qualified 1-butene products is 72 hours by adopting a traditional mode. It can be seen that the time for producing 1-butene can be effectively shortened by the method of the present invention.
According to the invention, the heavy four carbon in the production line is directly introduced into the 1-butene rectifying tower for directly producing 1-butene, so that the time for producing 1-butene is effectively prolonged. In the whole production process, the driving can be carried out without waiting for mixing four carbons, the driving time can be effectively shortened by reversing the driving, and the production efficiency is improved. And after the DMTO and olefin separation device produces qualified mixed carbon four, slowly cutting the feed from heavy carbon four to mixed carbon four for full-system start-up. Compared with the traditional preparation of qualified 1-butene products, the method provided by the invention requires only 24 hours, so that the production efficiency is effectively improved.
It will be apparent to those skilled in the art that various modifications and variations can be made to the present invention without departing from the spirit or scope of the invention. Thus, it is intended that the present invention also include such modifications and alterations insofar as they come within the scope of the appended claims or the equivalents thereof. The above-described embodiments are merely preferred embodiments for fully explaining the present invention, and the scope of protection is not limited thereto. Equivalent substitutions and modifications are intended to be within the scope of the present invention, as will be apparent to those skilled in the art based upon the present disclosure.

Claims (9)

1.一种MTBE-丁烯装置倒开车的方法，其特征在于，包括以下步骤：1. A method for reverse start-up of an MTBE-butene unit, characterized in that it comprises the following steps: 将混合碳四罐中的重四碳通过管线引入第一精馏塔内将轻组分脱除后，将第一精馏塔塔底的碳四馏分送至第二精馏塔，碳四馏分在第二精馏塔内进行分离，将重组分脱除后，第二精馏塔塔顶的部分气体经冷凝器冷凝后，作为1-丁烯送出，第二精馏塔塔底的正丁烷和2-丁烯送至异构化单元。The heavy C4 in the mixed C4 tank is introduced into the first distillation tower through a pipeline to remove the light components, and then the C4 fraction at the bottom of the first distillation tower is sent to the second distillation tower. The C4 fraction is separated in the second distillation tower. After the heavy components are removed, part of the gas at the top of the second distillation tower is condensed by a condenser and sent out as 1-butene, and the n-butane and 2-butene at the bottom of the second distillation tower are sent to the isomerization unit. 2.根据权利要求1所述的MTBE-丁烯装置倒开车的方法，其特征在于，所述第一精馏塔包括上塔和下塔；2. The method for reverse start-up of an MTBE-butene unit according to claim 1, characterized in that the first distillation tower comprises an upper tower and a lower tower; 所述下塔的气相物料通过管线进入上塔的底部，作为上升气相物流，所述上塔的液体通过中间泵送至下塔的顶部；The gaseous material of the lower tower enters the bottom of the upper tower through a pipeline as an ascending gaseous material flow, and the liquid of the upper tower is pumped to the top of the lower tower through an intermediate pump; 所述下塔的塔釜产物为脱掉异丁烷轻组分的碳四馏分，经塔底泵抽出，送至第二精馏塔。The bottom product of the lower tower is a C4 fraction from which the light component of isobutane has been removed, which is pumped out through a bottom pump and sent to a second distillation tower. 3.根据权利要求2所述的MTBE-丁烯装置倒开车的方法，其特征在于，所述第二精馏塔包括上段塔和下段塔；3. The method for reverse start-up of the MTBE-butene unit according to claim 2, characterized in that the second distillation tower comprises an upper tower and a lower tower; 所述上段塔顶部的气体经冷凝器冷凝后进入塔顶回流罐，再经回流泵加压后，一部分作为回流进入上段塔的塔顶，另一部分作为1-丁烯送出；The gas at the top of the upper tower is condensed by a condenser and enters a reflux tank at the top of the tower. After being pressurized by a reflux pump, a portion of the gas enters the top of the upper tower as reflux, and the other portion is sent out as 1-butene. 所述下段塔顶部的气相物料通过管线进入所述上段塔的底部，作为上升气相物流，所述上段塔釜液体通过中间泵送至所述下段塔顶部作内回流；所述下段塔的底部产出以正丁烷和丁烯-2为主的重馏分，经塔底泵抽出，送入2-丁烯冷却器冷却后，一部分送入异构化单元作为原料，另一部分作为副产品和异构化单元返回的重碳四混合后送出。The gaseous material at the top of the lower tower enters the bottom of the upper tower through a pipeline as an ascending gaseous material flow, and the liquid in the upper tower bottom is pumped to the top of the lower tower through an intermediate pump for internal reflux; the bottom of the lower tower produces a heavy fraction mainly composed of n-butane and butene-2, which is pumped out by a bottom pump, sent to a 2-butene cooler for cooling, and a part of it is sent to the isomerization unit as a raw material, and the other part is sent out as a by-product after being mixed with heavy carbon four returned from the isomerization unit. 4.根据权利要求3所述的MTBE-丁烯装置倒开车的方法，其特征在于，所述第一精馏塔的下塔与第二精馏塔的上段塔通过管线连通。4. The method for reverse start-up of an MTBE-butene unit according to claim 3, characterized in that the lower tower of the first distillation tower is connected to the upper tower of the second distillation tower through a pipeline. 5.根据权利要求2所述的MTBE-丁烯装置倒开车的方法，其特征在于，5. The method for reverse start-up of the MTBE-butene unit according to claim 2, characterized in that: 所述第一精馏塔上塔的压力范围为0.60MPa～0.65MPa，塔顶温度为45℃～55℃，塔底温度为65℃～80℃，塔顶回流比为1320；The pressure range of the upper tower of the first distillation tower is 0.60MPa-0.65MPa, the top temperature is 45°C-55°C, the bottom temperature is 65°C-80°C, and the top reflux ratio is 1320; 所述第一精馏塔下塔压力范围为0.65MPa～0.70MPa，塔顶温度为60℃～70℃，塔底温度为65℃～75℃。The lower tower pressure range of the first distillation tower is 0.65MPa-0.70MPa, the tower top temperature is 60℃-70℃, and the tower bottom temperature is 65℃-75℃. 6.根据权利要求3所述的MTBE-丁烯装置倒开车的方法，其特征在于，所述第二精馏塔上塔的压力范围为0.40MPa～0.50MPa，塔顶温度为42℃～52℃，塔底温度为46℃～56℃，塔顶回流比为28；6. The method for reverse start-up of the MTBE-butene unit according to claim 3, characterized in that the pressure range of the upper tower of the second distillation tower is 0.40MPa-0.50MPa, the tower top temperature is 42°C-52°C, the tower bottom temperature is 46°C-56°C, and the tower top reflux ratio is 28; 所述第二精馏塔下塔压力范围为0.45MPa～0.55MPa，塔顶温度为46℃～56℃，塔底温度为55℃～65℃。The lower tower pressure range of the second distillation tower is 0.45MPa-0.55MPa, the tower top temperature is 46°C-56°C, and the tower bottom temperature is 55°C-65°C. 7.根据权利要求1所述的MTBE-丁烯装置倒开车的方法，其特征在于，混合碳四罐中的重四碳具体来源过程如下：7. The method for reverse start-up of the MTBE-butene unit according to claim 1, characterized in that the specific source process of the heavy four carbons in the mixed carbon four tank is as follows: 将第二精馏塔的塔釜重碳四，通过管线分别与所述异构化单元和所述混合碳四罐连接。The heavy C4 in the bottom of the second distillation tower is connected to the isomerization unit and the mixed C4 tank through pipelines. 8.根据权利要求1所述的MTBE-丁烯装置倒开车的方法，其特征在于，所述重四碳包括正丁烷、顺-2-丁烯、反-2-丁烯和丁烯。8. The method for reverse start-up of an MTBE-butene unit according to claim 1, characterized in that the heavy four carbon atoms include n-butane, cis-2-butene, trans-2-butene and butene. 9.根据权利要求1所述的MTBE-丁烯装置倒开车的方法，其特征在于，还包括，待DMTO及烯烃分离装置产出合格混合碳四后，将重碳四替换为混合碳四并通过管线引入第一精馏塔后，进行全系统开车。9. The method for reverse start-up of the MTBE-butene unit according to claim 1 is characterized in that it also includes, after the DMTO and olefin separation units produce qualified mixed C4, replacing the heavy C4 with mixed C4 and introducing it into the first distillation tower through a pipeline, and then starting up the whole system.
CN202411326508.0A 2024-09-23 2024-09-23 Method for reversing and driving MTBE-butene device Pending CN119186000A (en)

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