CN109354567A - The isobutene lamination system device and coincidence process method converted by methyl tertiary butyl ether(MTBE) plant modification - Google Patents
The isobutene lamination system device and coincidence process method converted by methyl tertiary butyl ether(MTBE) plant modification Download PDFInfo
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- CN109354567A CN109354567A CN201811525210.7A CN201811525210A CN109354567A CN 109354567 A CN109354567 A CN 109354567A CN 201811525210 A CN201811525210 A CN 201811525210A CN 109354567 A CN109354567 A CN 109354567A
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- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 title claims abstract description 40
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims abstract description 36
- 230000008569 process Effects 0.000 title claims abstract description 23
- 238000003475 lamination Methods 0.000 title claims abstract description 17
- 238000012986 modification Methods 0.000 title claims abstract description 14
- 230000004048 modification Effects 0.000 title claims abstract description 14
- 239000003112 inhibitor Substances 0.000 claims abstract description 91
- 230000003197 catalytic effect Effects 0.000 claims abstract description 40
- 238000004821 distillation Methods 0.000 claims abstract description 40
- 238000011084 recovery Methods 0.000 claims abstract description 40
- 238000000605 extraction Methods 0.000 claims abstract description 27
- 238000006243 chemical reaction Methods 0.000 claims abstract description 19
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 18
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 18
- 238000002360 preparation method Methods 0.000 claims abstract description 13
- 239000000203 mixture Substances 0.000 claims abstract description 9
- 238000010992 reflux Methods 0.000 claims description 22
- 239000000047 product Substances 0.000 claims description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 19
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 13
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 12
- 239000000463 material Substances 0.000 claims description 11
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 claims description 8
- 239000004263 Guaiac resin Substances 0.000 claims description 5
- 239000011692 calcium ascorbate Substances 0.000 claims description 5
- 238000000746 purification Methods 0.000 claims description 5
- 230000001629 suppression Effects 0.000 claims description 4
- 239000000945 filler Substances 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 3
- 229920005862 polyol Polymers 0.000 claims description 3
- 150000003077 polyols Chemical class 0.000 claims description 3
- 239000002446 δ-tocopherol Substances 0.000 claims description 3
- 239000000574 octyl gallate Substances 0.000 claims description 2
- 239000000737 potassium alginate Substances 0.000 claims description 2
- 230000007115 recruitment Effects 0.000 claims description 2
- 239000000661 sodium alginate Substances 0.000 claims description 2
- 239000013589 supplement Substances 0.000 claims description 2
- 239000003795 chemical substances by application Substances 0.000 claims 2
- 230000005764 inhibitory process Effects 0.000 claims 1
- 239000000284 extract Substances 0.000 abstract description 6
- 238000004519 manufacturing process Methods 0.000 abstract description 6
- 239000003502 gasoline Substances 0.000 abstract description 5
- 230000006872 improvement Effects 0.000 abstract description 4
- 239000002994 raw material Substances 0.000 abstract description 4
- 150000001336 alkenes Chemical class 0.000 abstract description 3
- 238000002156 mixing Methods 0.000 abstract description 3
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract description 3
- 239000000470 constituent Substances 0.000 abstract description 2
- 125000000959 isobutyl group Chemical group [H]C([H])([H])C([H])(C([H])([H])[H])C([H])([H])* 0.000 abstract description 2
- 238000004064 recycling Methods 0.000 abstract 1
- 235000019441 ethanol Nutrition 0.000 description 7
- DFVOXRAAHOJJBN-UHFFFAOYSA-N 6-methylhept-1-ene Chemical compound CC(C)CCCC=C DFVOXRAAHOJJBN-UHFFFAOYSA-N 0.000 description 4
- DKGAVHZHDRPRBM-UHFFFAOYSA-N Tert-Butanol Chemical compound CC(C)(C)O DKGAVHZHDRPRBM-UHFFFAOYSA-N 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 230000009466 transformation Effects 0.000 description 3
- 238000001816 cooling Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000005457 optimization Methods 0.000 description 2
- 230000002159 abnormal effect Effects 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 239000002551 biofuel Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- -1 methyl tertbutyl Chemical group 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 238000003809 water extraction Methods 0.000 description 1
- 239000002076 α-tocopherol Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/02—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons
- C07C2/04—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation
- C07C2/06—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation of alkenes, i.e. acyclic hydrocarbons having only one carbon-to-carbon double bond
- C07C2/08—Catalytic processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/10—Liquid carbonaceous fuels containing additives
- C10L1/14—Organic compounds
- C10L1/16—Hydrocarbons
- C10L1/1608—Well defined compounds, e.g. hexane, benzene
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L10/00—Use of additives to fuels or fires for particular purposes
- C10L10/10—Use of additives to fuels or fires for particular purposes for improving the octane number
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present patent application provides a kind of isobutene lamination system device converted by methyl tertiary butyl ether(MTBE) plant modification and coincidence process method.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
Technical field
The present invention relates to mix carbon four as raw material, the gasoline alkylate tempered oil of isooctene antiknock component is prepared
System and device and preparation method.
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 of 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 present patent application 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 and coincidence process method of ether plant modification conversion.
The isobutene lamination system device technique side converted by methyl tertiary butyl ether(MTBE) plant modification that the present patent application provides
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 the purification of the carbon four feed branch of material mixer front end and inhibitor is fed branch, the purification feed of carbon four
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 raw polyol
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 heat exchange of the first charging-product
Device is exported to catalytic distillation unit；Superposition reactor feeding pipe road has assembled mixer, and the one of the mixer enters
Material channel is connected to material mixer, and another feeding channel is the first reflux branch that superposition reactor discharge port is drawn, this time
Stream 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 product discharge pipeline and exports through cooler extremely
Inhibitor recovery unit, tower bottom overlap and have assembled the second charging-product exchanger, product cooler on product discharge pipeline
And column bottoms pump, overhead pipeline are connected to return tank through condenser, are connected on return tank and are back to by reflux pump driving
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 inhibitor
Rectifying recovery tower connection composition, inhibitor extract column overhead and connect heat bodied oil discharge nozzle, and tower bottom is returned through depickling clarifier, inhibitor
Tower charging flash tank, inhibitor pump and inhibitor is received to feed-extract water- to-water heat exchanger and connect with inhibitor rectifying recovery tower feed inlet,
Inhibitor rectifying recovery tower tower bottom extraction inhibited dose of charging of water lines-extraction water- to-water heat exchanger and extraction water cooler are connected to suppression
Preparation extracts tower packing top, and inhibitor rectifying recycles column overhead discharge nozzle road and connects inhibitor return tank, inhibitor return tank
Inhibitor reflux branch road between inhibitor rectifying recovery tower tower item has assembled inhibitor reflux pump.
The present patent application also provides a kind of based on isobutene lamination system device implementation coincidence process method.This overlapping
Process are as follows:
1. building-up reactions
Wherein inhibitor inlet amount accounts for the 1.0-1.5% of total feed, and the reaction condition of 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℃ |
2. catalytic distillation
Catalytic distillation tower C301 reaction condition:
| Title | Quantity |
| 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 |
3. inhibitor recycles
The reaction condition of inhibitor extraction tower C302 therein:
| 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 |
Inhibitor rectifying recovery tower C303 process conditions therein:
| 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 |
The disclosed isobutene lamination system device converted by methyl tertiary butyl ether(MTBE) plant modification of present patent application and overlapping
Process technical solution, technological merit are: with the smallest improvement cost, i.e., maximum optimization system device and process facility
Transformation determines with the design of coincidence process method, realize play to greatest extent former methyl tertiary butyl ether(MTBE) preparation system device and its
The application value of process facility, efficient completion mixing carbon four are that the isobutyl olefinic constituents overlapping production of raw material prepares high-octane rating
The olefin(e) centent of isooctene, heat bodied oil is greater than 90%, meets directly as gasoline concoction component, maximizes 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 purifies
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 feed
Branch: the charging by primitive nail raw polyol tank and metering pump as inhibitor head tank D303 and the metering pump P302 inhibitor tert-butyl alcohol
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, take two superposition reactor R302/1,
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 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 is whole
In body system and 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 |
It is cooling through the second charging-product exchanger E302 and product that catalytic distillation tower C301 tower bottom overlaps the output of product discharge pipeline
Device E311, column bottoms pump P403 are exported to inhibitor recovery unit, and the second charging-product exchanger E302 therein is anti-by overlapping
It answers device R302/1, R302/2 discharge port to distillate to catalytic distillation tower C301 charging and catalytic distillation tower C301 tower bottom to change between material
Heat.Catalytic distillation tower C301 overhead pipeline is connected to return tank D304 through condenser E307, connects on return tank D304
There is the second reflux branch that catalytic distillation tower C301 tower top is back to by reflux pump P303 driving；Its reflux ratio is as illustrated above；
Catalytic distillation tower C301 is additionally provided with inhibitor supplement pipeline, and inhibited dose of clarifier D309 is connected with inhibitor head tank D303,
It is connected to catalytic distillation tower C301 conversion zone；
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 as suppression
Preparation rectifying recovery tower C303 connection composition, inhibitor extraction tower C302 tower top connect heat bodied oil discharge nozzle, heat bodied oil discharge nozzle
It is connected with overlapping oil tank D307 and overlapping oil pump P307, the column bottoms pump with catalytic distillation tower C301 tower bottom overlapping product discharge pipeline
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 is that Methanol Recovery feeds the inhibitor recovery tower charging flash tank D305 of flash tank, is originally first through depickling clarifier D401, originally
The inhibitor pump P304 and primitive nail alcohol of alcohol feed pump feed-inhibitor for extracting water- to-water heat exchanger is fed-and extract water- to-water heat exchanger E314
Connect with inhibitor rectifying recovery tower C303 feed inlet, inhibitor rectifying recovery tower C303 tower bottom extract inhibited dose of water lines into
Material-extraction water- to-water heat exchanger E314 and extraction water cooler E309 is connected to inhibitor extraction tower C302 filler top, inhibitor essence
It evaporates after inhibited dose of charging of recovery tower C303 tower bottom extraction water-extraction water- to-water heat exchanger E314 is cooled to 90 DEG C, then through extracting water cooling
But device 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 |
Inhibitor rectifying recovery tower C303 tower top discharging piping connection inhibitor return tank D306, inhibitor return tank D306 and suppression
Inhibitor reflux branch road between preparation rectifying recovery tower C303 tower item has assembled inhibitor reflux pump P306.Inhibitor
Inhibitor is separated from water in rectifying recovery tower C303, process conditions are as shown in the table, tower top inhibitor water content bottom 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 (6)
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:
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.
5. a kind of based on any isobutene lamination system converted by methyl tertiary butyl ether(MTBE) plant modification of claim 1-4
The coincidence process method that device is implemented, it is characterised in that this coincidence process method are as follows:
1. building-up reactions
Wherein inhibitor inlet amount accounts for the 1.0-1.5% of total feed, and the reaction condition of superposition reactor is:
2. catalytic distillation
Catalytic distillation tower C301 reaction condition:
3. inhibitor recycles
The reaction condition of inhibitor extraction tower C302 therein:
Inhibitor rectifying recovery tower C303 process conditions therein:
。
6. coincidence process method according to claim 5, which is characterized in that this coincidence process method are as follows: catalytic distillation tower
Inhibitor magnitude of recruitment is the 1.0% ~ 1.5% of inlet amount weight.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811525210.7A CN109354567B (en) | 2018-12-13 | 2018-12-13 | Superposition process method of isobutene superposition system device reconstructed by methyl tertiary butyl ether device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811525210.7A CN109354567B (en) | 2018-12-13 | 2018-12-13 | Superposition process method of isobutene superposition system device reconstructed by methyl tertiary butyl ether device |
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| CN113058283A (en) * | 2021-03-01 | 2021-07-02 | 中国石油化工股份有限公司 | Methanol recovery system and process of MTBE (methyl tert-butyl ether) device |
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