CN209276413U - The isobutene lamination system device converted by methyl tertiary butyl ether(MTBE) plant modification - Google Patents

The isobutene lamination system device converted by methyl tertiary butyl ether(MTBE) plant modification Download PDF

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Publication number
CN209276413U
CN209276413U CN201822092683.4U CN201822092683U CN209276413U CN 209276413 U CN209276413 U CN 209276413U CN 201822092683 U CN201822092683 U CN 201822092683U CN 209276413 U CN209276413 U CN 209276413U
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Prior art keywords
inhibitor
tower
unit
catalytic distillation
pump
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CN201822092683.4U
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Inventor
吕晓东
孙方宪
朱淑军
张春峰
刘成军
段宏毅
车平生
温世昌
管秀明
赵实柱
赵霞
周璇
王晓芳
李倞琛
高青
陈常蕊
刘晓林
郭佳林
丛培鑫
刑正奎
阚伟
李山明
韩晓辉
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ZIBO QIXIAN TENGDA CHEMICAL CO Ltd
DANDONG MINGZHU SPECIAL TYPE RESIN Co Ltd
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ZIBO QIXIAN TENGDA CHEMICAL CO Ltd
DANDONG MINGZHU SPECIAL TYPE RESIN Co Ltd
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    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/10Process efficiency

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Abstract

The utility model provides a kind of isobutene lamination system device converted by methyl tertiary butyl ether(MTBE) plant modification.Its isobutene lamination system device is by feed unit, Superposition unit, catalytic distillation unit and inhibitor recovery unit composition, inhibitor recovery unit therein is connected with inhibitor rectifying recovery tower by inhibitor extraction tower and is formed, carbon four and inhibitor are mixed in superposition reactor pre-reaction, again through catalytic distillation tower depth building-up reactions, inhibited dose of extraction tower and inhibitor rectifying recovery tower complete inhibitor recycling again and overlapping product extracts, with the smallest improvement cost, the application value of former methyl tertiary butyl ether(MTBE) preparation system device and its process facility is played to greatest extent, it is efficient to complete the isobutyl olefinic constituents overlapping production that mixing carbon four is raw material, the olefin(e) centent of heat bodied oil is greater than 90%, meet directly as gasoline concoction component.

Description

The isobutene lamination system device converted by methyl tertiary butyl ether(MTBE) plant modification
Technical field
The utility model relates to mix carbon four as raw material, prepare the blending of the gasoline alkylate of isooctene antiknock component The system and device and preparation method of oil.
Background technique
The joint publication of 15 ministries and commissions such as National Development and Reform Committee " produces and promotes the use of vehicle ethanol about bio-fuel ethyl alcohol is expanded The embodiment of gasoline ", determine that multiple provinces and cities, 2017 China Nian Qi promote the use of ethanol petrol, and realize national base in the year two thousand twenty This all standing.Based on current law, methyl tertiary butyl ether(MTBE) halt production is for the important technical task that petroleum chemical enterprise faces Conversion could be transformed in the application new way and existing methyl tertiary butyl ether(MTBE) preparation system device for developing isobutene to greatest extent again It recycles.In the prior art, occurred being changed by original methyl tertiary butyl ether(MTBE) system and device different for isobutene overlapping production two The technical solution of butylene (isooctene), but generally existing transformation involves that wide, range is big, especially new coincidence process method and former Process facility is difficult to match, and leads to the abnormal height of improvement cost, it is difficult to meet the operation and development needs of fast transformation.
Summary of the invention
The goal of the invention of the utility model is to play former methyl tertiary butyl ether(MTBE) to greatest extent with the smallest improvement cost Preparation system device and its process facility effect, for completing to mix carbon four as the isobutene overlapping production preparation Gaoxin of raw material Alkane value isooctene, product meet the technical requirement directly as gasoline concoction component, and provide one kind by methyl tertbutyl The isobutene lamination system device of ether plant modification conversion.
The isobutene lamination system device technique side provided by the utility model converted by methyl tertiary butyl ether(MTBE) plant modification Case, main technical content are: a kind of isobutene lamination system device converted by methyl tertiary butyl ether(MTBE) plant modification, by preparation Process, the composition of this system device include feed unit, Superposition unit, catalytic distillation unit and inhibitor recovery unit, wherein :
1. feed unit
This feed unit is that the purification of the carbon four feed branch of material mixer front end and inhibitor are fed branch, and carbon four purifies Feed branch includes four head tank of carbon, the pump of carbon four and is separated by filtration dehydrator and connects composition;Inhibitor is fed branch: by primitive nail alcohol Head tank and metering pump are as inhibitor head tank and metering pump;
2. Superposition unit
Superposition unit: being superposition reactor by former methyltertiarvbutyl ether reactor, and superposition reactor discharges pipeline through the first charging-product Heat exchanger is exported to catalytic distillation unit;Superposition reactor feeding pipe road has assembled mixer, the mixer One feeding channel is connected to material mixer, and another feeding channel is the first reflux branch that superposition reactor discharge port is drawn, The reflux branch road has assembled recirculation cooler and circulating pump;
3. catalytic distillation unit
Catalytic distillation unit is made of catalytic distillation tower, and catalytic distillation tower tower bottom overlaps the output of product discharge pipeline through cooling It is cold that device to inhibitor recovery unit, on tower bottom overlapping product discharge pipeline has assembled the second charging-product exchanger, product But device and column bottoms pump, overhead pipeline are connected to return tank through condenser, are connected on return tank and are driven back by reflux pump It flow to the second reflux branch of catalytic distillation column overhead;
4. inhibitor recovery unit
Inhibitor recovery unit is by primitive nail alcohol extraction tower as inhibitor extraction tower and former methanol rectification recovery tower as suppression Preparation rectifying recovery tower connection composition, inhibitor extract column overhead and connect heat bodied oil discharge nozzle, and tower bottom is through depickling clarifier, inhibition Agent recovery tower charging flash tank, inhibitor pump and inhibitor feed-extract water- to-water heat exchanger and inhibitor rectifying recovery tower feed inlet Connection, inhibitor rectifying recovery tower tower bottom extracts inhibited dose of charging of water lines-extraction water- to-water heat exchanger and extraction water cooler connects It is connected to inhibitor extraction tower packing top, inhibitor rectifying recycles column overhead discharge nozzle road and connects inhibitor return tank, inhibitor Inhibitor reflux branch road between return tank and inhibitor rectifying recovery tower tower item has assembled inhibitor reflux pump.
The disclosed isobutene lamination system device technique side converted by methyl tertiary butyl ether(MTBE) plant modification of present patent application Case, technological merit are: with the smallest improvement cost, i.e., maximum optimization system device and process facility transformation and coincidence process The design of method determines, realizes the application for playing former methyl tertiary butyl ether(MTBE) preparation system device and its process facility to greatest extent Value, efficient completion mixing carbon four are that the isobutyl olefinic constituents overlapping production of raw material prepares high-octane rating isooctene, heat bodied oil Olefin(e) centent be greater than 90%, meet directly as gasoline concoction component, maximize enterprise management efficiency.
Detailed description of the invention
Fig. 1, Fig. 2, which connect total constitute with the system and device that Fig. 3 is present patent application, to scheme.
Specific embodiment
The disclosed isobutene lamination system device converted by methyl tertiary butyl ether(MTBE) plant modification of present patent application, is to be based on Former methyl tertiary butyl ether(MTBE) device and former etherificate production technology and facility, and the new building-up reactions method of matching design met and Higher than the alkyl overlapping blending oil product of requirements of the national standard, implemented between original system device and process implementing with maximally utilizing Optimization selection technical purpose.
By preparation flow, the composition of this isobutene lamination system device includes feed unit, Superposition unit, catalytic distillation list Member and inhibitor recovery unit, it is therein
1. feed unit
This feed unit is that the purification of the carbon four feed branch of the front end material mixer M301 and inhibitor are fed branch.Carbon four Purification feed branch includes that four head tank D302 of carbon, carbon four pump P301 and with dehydrator D301 is separated by filtration connects composition;Inhibitor It is fed branch: by primitive nail raw polyol tank and metering pump as inhibitor head tank D303 and the metering pump P302 inhibitor tert-butyl alcohol Inlet amount accounts for the 1.0-1.5% of carbon four and inhibitor charging sum total;
2. Superposition unit
It is superposition reactor by former methyltertiarvbutyl ether reactor.In this implementation system apparatus arrangements, two superposition reactor R302/ are taken 1, R302/2 composes in parallel structure, facilitates and is needed flexibly add one group of overlapping pre-reaction of increasing according to practical preparative-scale, and It can match with the process scale of postorder flow path device, or according to the operation needs such as maintenance, two superposition reactor rotations access In total system device.
Superposition reactor discharging pipeline is exported through the first charging-product exchanger E302 to catalytic distillation unit;Two overlappings Reactor R302/1, R302/2 feeding pipe road has respectively assembled mixer M401, M402, the mixer M401, A feeding channel of M402 is connected to material mixer M301, and another feeding channel is that superposition reactor R302/1, R302/2 go out The first reflux branch that material mouth is drawn, the first reflux branch road have assembled recirculation cooler E401, E402 and circulating pump P401, P402, circulating reflux ratio are 2, and the reaction process condition of this superposition reactor is:
Title Quantity Remarks
Feeding temperature 35~50 DEG C
Outlet temperature 55~60℃ Not more than 80 DEG C
Inlet pressure; 0.8~1.0 MPaG
Outlet pressure; 0.65~0.9 MPaG It is controlled by the voltage-controlled system of catalytic distillation tower
Material reflux cycle ratio 2
Recirculation cooler output temperature 40℃
3. catalytic distillation unit
Catalytic distillation unit is made of catalytic distillation tower C301, and catalytic distillation tower C301 reaction condition is as shown in the table:
Title Quantity Remarks
Tower top pressure 0.5~0.7 MPaG
Tower top temperature 55~65℃
Column bottom temperature 190~198℃
Tower reflux ratio Weight ratio is 1.0
Tower mends inhibitor 150 kg/h
Inhibitor magnitude of recruitment 1.0%~1.5% For the weight percent of inlet amount
Catalytic distillation tower C301 tower bottom overlaps the output of product discharge pipeline through the second charging-product exchanger E302 and product Cooler E311, column bottoms pump P403 are exported to inhibitor recovery unit, and the second charging-product exchanger E302 therein is by folding Reactor R302/1, R302/2 discharge port is closed to distillate between material to catalytic distillation tower C301 charging and catalytic distillation tower C301 tower bottom Heat exchange.Catalytic distillation tower C301 overhead pipeline is connected to return tank D304 through condenser E307, connects on return tank D304 It is connected to the second reflux branch that catalytic distillation tower C301 tower top is back to by reflux pump P303 driving;Its reflux ratio table as above is aobvious Show;Catalytic distillation tower C301 is additionally provided with inhibitor supplement pipeline, inhibited dose of clarifier D309 and inhibitor head tank D303 phase Even, it is connected to catalytic distillation tower C301 conversion zone;
4. inhibitor recovery unit
Inhibitor recovery unit is made by primitive nail alcohol extraction tower as inhibitor extraction tower C302 and former methanol rectification recovery tower For inhibitor rectifying recovery tower C303 connection composition, inhibitor extraction tower C302 tower top connects heat bodied oil discharge nozzle, and heat bodied oil goes out Expects pipe is connected with overlapping oil tank D307 and overlapping oil pump P307, the tower with catalytic distillation tower C301 tower bottom overlapping product discharge pipeline Bottom pumps P403 cooperation, to meet the power that washing is needed from the discharging of catalytic distillation tower C301 tower reactor.Inhibitor extraction tower C302 tower bottom through depickling clarifier D401, be originally Methanol Recovery charging flash tank inhibitor recovery tower charging flash tank D305, It originally was that the inhibitor pump P304 of methanol feed pump and primitive nail alcohol feed-extract the inhibitor charging of water- to-water heat exchanger-extraction water heat exchange Device E314 is connect with inhibitor rectifying recovery tower C303 feed inlet, and inhibitor rectifying recovery tower C303 tower bottom extracts water lines through pressing down Preparation feeds-extracts water- to-water heat exchanger E314 and extraction water cooler E309 is connected to inhibitor extraction tower C302 filler top, presses down After inhibited dose of charging of preparation rectifying recovery tower C303 tower bottom extraction water-extraction water- to-water heat exchanger E314 is cooled to 90 DEG C, then through extracting Water intaking cooler E309 is cooled to 40 DEG C, is sent into inhibitor extraction tower C302 filler top.
The reaction condition of inhibitor extraction tower C302:
Title Quantity
Pan feeding temperature 40℃
Tower top pressure 0.5~0.6 MPaG
Tower bottom pressure 0.6~0.75 MPaG
Water oil weight ratio 1:2
The discharging of inhibitor rectifying recovery tower C303 tower top piping connection inhibitor return tank D306, inhibitor return tank D306 Inhibitor reflux branch road between inhibitor rectifying recovery tower C303 tower item has assembled inhibitor reflux pump P306.Suppression Inhibitor is separated from water in preparation rectifying recovery tower C303, process conditions are as shown in the table, tower top inhibitor water content Bottom is in 15.0% (m/m):
Title Quantity
Tower top pressure Normal pressure~0.1 MPaG
Tower top temperature 75 ~ 90 DEG C, preferably 79 DEG C
Column bottom temperature 100 ~ 120 DEG C, preferably 102 DEG C
Flow back weight ratio 3~5
By the isobutene lamination system device after former methyl tertiary butyl ether(MTBE) plant modification, olefin(e) centent in obtained heat bodied oil Greater than 90%, meet tempered oil technical requirement.

Claims (4)

1. a kind of isobutene lamination system device converted by methyl tertiary butyl ether(MTBE) plant modification, by preparation flow, this system dress The composition set includes feed unit, Superposition unit, catalytic distillation unit and inhibitor recovery unit, which is characterized in that therein:
1. feed unit
This feed unit is that the purification of the carbon four feed branch of the front end material mixer (M301) and inhibitor are fed branch, carbon four Purification feed branch include four head tank of carbon (D302), carbon four pump (P301) and be separated by filtration dehydrator (D301) connection form; Inhibitor is fed branch: by primitive nail raw polyol tank and metering pump as inhibitor head tank (D303) and metering pump (P302);
2. Superposition unit
It is superposition reactor by former methyltertiarvbutyl ether reactor, superposition reactor discharges pipeline through the first charging-product exchanger (E302) It exports to catalytic distillation unit;Superposition reactor feeding pipe road has assembled mixer, a pan feeding of the mixer Channel is connected to material mixer, and another feeding channel is the first reflux branch that superposition reactor discharge port is drawn, and first time Stream branch road has assembled recirculation cooler and circulating pump;
3. catalytic distillation unit
Catalytic distillation unit is made of catalytic distillation tower (C301), and it is defeated that catalytic distillation tower (C301) tower bottom overlaps product discharge pipeline Out through cooler to inhibitor recovery unit, tower bottom, which overlaps, has assembled the heat exchange of the second charging-product on product discharge pipeline Device (E302), product cooler (E311) and column bottoms pump (P403), overhead pipeline are connected to return tank through condenser (D304), it is connected on return tank (D304) and is back to the second of catalytic distillation tower (C301) tower top by reflux pump (P303) driving Flow back branch;
4. inhibitor recovery unit
Inhibitor recovery unit is by primitive nail alcohol extraction tower as inhibitor extraction tower (C302) and former methanol rectification recovery tower conduct Inhibitor rectifying recovery tower (C303) connection composition, inhibitor extraction tower (C302) tower top connect heat bodied oil discharge nozzle, tower bottom warp Depickling clarifier (D401), inhibitor recovery tower charging flash tank (D305), inhibitor pump (P304) and inhibitor charging-extraction Water- to-water heat exchanger (E314) is connect with inhibitor rectifying recovery tower (C303) feed inlet, inhibitor rectifying recovery tower (C303) tower bottom extraction Water intaking inhibited dose of charging of pipeline-extraction water- to-water heat exchanger (E314) and extraction water cooler (E309) are connected to inhibitor extraction tower (C302) filler top, inhibitor rectifying recovery tower (C303) tower top discharge piping connection inhibitor return tank (D306), inhibit Inhibitor reflux branch road between agent return tank (D306) and inhibitor rectifying recovery tower (C303) tower item has assembled suppression Preparation reflux pump (P306).
2. the isobutene lamination system device according to claim 1 converted by methyl tertiary butyl ether(MTBE) plant modification, special Sign is that catalytic distillation tower (C301) conversion zone is connected with inhibitor supplement pipeline, inhibited dose of clarifier (D309) and inhibition Agent head tank (D303) is connected.
3. the isobutene lamination system device according to claim 1 or 2 converted by methyl tertiary butyl ether(MTBE) plant modification, It is characterized in that, two superposition reactors (R302/1, R302/2) is taken to compose in parallel structure, two superposition reactors (R302/1, R302/2) feeding pipe road has respectively assembled mixer (M401, M402), the reflux of the mixer (M401, M402) Branch road has assembled recirculation cooler (E401, E402) and circulating pump (P401, P402).
4. the isobutene lamination system device according to claim 1 or 2 converted by methyl tertiary butyl ether(MTBE) plant modification, It is characterized in that, heat bodied oil discharge nozzle is connected with overlapping oil tank (D307) and overlaps product discharge with catalytic distillation tower (C301) tower bottom The overlapping oil pump (P307) of column bottoms pump (P403) the power cooperation of pipeline.
CN201822092683.4U 2018-12-13 2018-12-13 The isobutene lamination system device converted by methyl tertiary butyl ether(MTBE) plant modification Active CN209276413U (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109354567A (en) * 2018-12-13 2019-02-19 丹东明珠特种树脂有限公司 The isobutene lamination system device and coincidence process method converted by methyl tertiary butyl ether(MTBE) plant modification

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109354567A (en) * 2018-12-13 2019-02-19 丹东明珠特种树脂有限公司 The isobutene lamination system device and coincidence process method converted by methyl tertiary butyl ether(MTBE) plant modification
CN109354567B (en) * 2018-12-13 2023-11-10 丹东明珠特种树脂有限公司 Superposition process method of isobutene superposition system device reconstructed by methyl tertiary butyl ether device

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