WO2009133423A1 - Industrial process for the preparation of diisopropyl either (dipe) - Google Patents

Industrial process for the preparation of diisopropyl either (dipe) Download PDF

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Publication number
WO2009133423A1
WO2009133423A1 PCT/IB2008/001121 IB2008001121W WO2009133423A1 WO 2009133423 A1 WO2009133423 A1 WO 2009133423A1 IB 2008001121 W IB2008001121 W IB 2008001121W WO 2009133423 A1 WO2009133423 A1 WO 2009133423A1
Authority
WO
WIPO (PCT)
Prior art keywords
reactor
high efficiency
etherification
hydration
diisopropyl ether
Prior art date
Application number
PCT/IB2008/001121
Other languages
French (fr)
Inventor
Rosario Rocco Tulino
Santino Letizia
Original Assignee
Rosario Rocco Tulino
Santino Letizia
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Rosario Rocco Tulino, Santino Letizia filed Critical Rosario Rocco Tulino
Priority to PCT/IB2008/001121 priority Critical patent/WO2009133423A1/en
Publication of WO2009133423A1 publication Critical patent/WO2009133423A1/en

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
    • C07C41/01—Preparation of ethers
    • C07C41/09—Preparation of ethers by dehydration of compounds containing hydroxy groups
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
    • B01J8/0257—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical in a cylindrical annular shaped bed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0278—Feeding reactive fluids
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/03—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by addition of hydroxy groups to unsaturated carbon-to-carbon bonds, e.g. with the aid of H2O2
    • C07C29/04—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by addition of hydroxy groups to unsaturated carbon-to-carbon bonds, e.g. with the aid of H2O2 by hydration of carbon-to-carbon double bonds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00002—Chemical plants
    • B01J2219/00004—Scale aspects
    • B01J2219/00006—Large-scale industrial plants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00002—Chemical plants
    • B01J2219/00027—Process aspects
    • B01J2219/0004—Processes in series
    • 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
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/582—Recycling of unreacted starting or intermediate materials

Definitions

  • the industrial attention is focalized on two starting gases: the butane from which the methyl tertiary butyl ether (MBTE) derives and the propylene from which the diisopropyl ether (DIPE) derives.
  • MBTE methyl tertiary butyl ether
  • DIPE diisopropyl ether
  • DIPE DIPE according to the enclosed scheme (see Fig. 1), developed in the process DIPE-R2 (see Fig. 2) according to the technology of appropriately catalyzed reactors (see Fig. 3) allows a structural simplification as it works at not elevated pressures and temperatures; consequently the plant cost is lower while there is a high production efficiency and a more simple and reliable plant management.
  • the raw materials, water and propylene are introduced, with pressure between 15 and 145 bar and temperature between 75°C and 380 0 C, into the hydration reactor

Abstract

Industrial production process of large quantities of diisopropyl ether using the propylene coming out from the crude oil refining, using catalyzed reactors at high efficiency, working at medium pressures and temperatures, thus allowing plant simplifications.

Description

DESCRIPTION
INDUSTRIAL PROCESS FOR THE PREPARATION OF DIISOPROPYL EITHER (DIPE)
of the industrial invention bearing the title
"Industrial production process, called DIPE-R2, for diisopropyl ether compound through catalytic reactors"
During the next decade it is forecast an increasing request of oxygenates to add to vehicle fuels. The basic components of these reformulated oxygenates are the ethers that are obtained starting from the gases available in large quantities from refineries.
The industrial attention is focalized on two starting gases: the butane from which the methyl tertiary butyl ether (MBTE) derives and the propylene from which the diisopropyl ether (DIPE) derives.
From the point of view of final use, the two products show similar characteristics so that they can be assumed (beside the mixing proportions) interchangeable.
The industrial production of MTBE requires instead very big reactors (up to 80 meter high), working under severe conditions of pressure and temperature
(ETHERMAX technology) with consequent high plant cost (see Fig. 4).
The production of DIPE according to the enclosed scheme (see Fig. 1), developed in the process DIPE-R2 (see Fig. 2) according to the technology of appropriately catalyzed reactors (see Fig. 3) allows a structural simplification as it works at not elevated pressures and temperatures; consequently the plant cost is lower while there is a high production efficiency and a more simple and reliable plant management.
The raw materials, water and propylene, are introduced, with pressure between 15 and 145 bar and temperature between 75°C and 3800C, into the hydration reactor
Rl (see Fig. 3). Inside the reactor, water and propylene cross the high efficiency catalyst obtaining diisopropyl ether, isopropyl alcohol and not reacted water. Inside the etherification reactor R2, working at temperature between 900C and 196°C and pressure between 4,5 and 86 bar, the isopropyl alcohol (IPA) is continuously converted, with high efficiency, to diisopropyl ether through the zeolite β (65%) plus alumina catalyst (see Fig. 3).
The chemical reactions inside the reactors, even they are optimized at very high efficiency, require a reagents recycling through phase separators (see Fig. 2). Basically the process consists of hydration reactor Rl and etherification reactor R2 catalyzed with zeolites. The other equipments are used only for the full reuse of intermediate products; consequently according to the plant capacity, they might have different characteristics because they don't have an importance in the chemical dynamic of the process but only a physical expansion more or less important, therefore their description is omitted because it is not innovative.

Claims

1) CLAIM 1: we claim a system of catalytic reactors for the industrial production of diisopropyl ether, composed by a hydration reactor and an etherification reactor
2) CLAIM 2 we claim a hydration reactor AS CLAIMED IN CLAIM 1, made with carbon steel, at annular chamber and tangential input, modular construction, catalyzed with zeolite ZSM 5, with high efficiency
3) CLAIM 3: we claim a hydration reactor AS CLAIMED IN CLAIM 2 working at pressure between 15 and 145 bar and temperature between 750C and 3800C
4) CLAIM 4: we claim an etherification reactor at high efficiency AS CLAIMED IN CLAIM 1 transforming the isopropyl alcohol (IPA) to diisopropyl ether through the zeolite β (65%) plus alumina catalyst
5) CLAIM 5: we claim an etherification reactor AS CLAIMED IN CLAIM 4 working at pressure between 4,5 and 86 bar and temperature between 900C and 196°C
6) CLAIM 6: we claim that the high efficiency of the etherification reactor CLAIMED IN CLAIM 4 is kept for every and all concentrations of isopropyl alcohol (IPA) arriving from the distilling apparatus as the reactor adjusts itself duly varying all the parameters within the settled range
7) CLAIM 7: we claim the configuration and the modular construction of the hydration reactor and of the etherification reactor CLAIMED IN ALL THE PREVIOUS CLAIMS 1-2-3-4-5-6 that consequently allow a more flexible and simple plant with a remarkably lower production total cost when compared to other oxygenates available in the market (about one eight in a plant with 1 million barrels production capacity)
PCT/IB2008/001121 2008-04-30 2008-04-30 Industrial process for the preparation of diisopropyl either (dipe) WO2009133423A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/IB2008/001121 WO2009133423A1 (en) 2008-04-30 2008-04-30 Industrial process for the preparation of diisopropyl either (dipe)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/IB2008/001121 WO2009133423A1 (en) 2008-04-30 2008-04-30 Industrial process for the preparation of diisopropyl either (dipe)

Publications (1)

Publication Number Publication Date
WO2009133423A1 true WO2009133423A1 (en) 2009-11-05

Family

ID=40225577

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/IB2008/001121 WO2009133423A1 (en) 2008-04-30 2008-04-30 Industrial process for the preparation of diisopropyl either (dipe)

Country Status (1)

Country Link
WO (1) WO2009133423A1 (en)

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4886918A (en) * 1988-11-07 1989-12-12 Mobil Oil Corporation Olefin hydration and etherification process employing serially staged olefin introduction
WO1990008124A1 (en) * 1989-01-12 1990-07-26 Mobil Oil Corporation Conversion of olefins to ethers
US5144086A (en) * 1991-05-06 1992-09-01 Mobil Oil Corporation Ether production
US5208387A (en) * 1991-12-27 1993-05-04 Mobil Oil Corporation Two stage process for production of diisopropyl ether
US5324866A (en) * 1993-03-23 1994-06-28 Uop Integrated process for producing diisopropyl ether from isopropyl alcohol
EP0733615A1 (en) * 1995-03-20 1996-09-25 Uop Process for producing diisopropyl ether
US5744645A (en) * 1994-09-26 1998-04-28 Uop Two-stage process for producing diisopropyl ether using catalytic distillation

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4886918A (en) * 1988-11-07 1989-12-12 Mobil Oil Corporation Olefin hydration and etherification process employing serially staged olefin introduction
WO1990008124A1 (en) * 1989-01-12 1990-07-26 Mobil Oil Corporation Conversion of olefins to ethers
US5144086A (en) * 1991-05-06 1992-09-01 Mobil Oil Corporation Ether production
US5208387A (en) * 1991-12-27 1993-05-04 Mobil Oil Corporation Two stage process for production of diisopropyl ether
US5324866A (en) * 1993-03-23 1994-06-28 Uop Integrated process for producing diisopropyl ether from isopropyl alcohol
US5744645A (en) * 1994-09-26 1998-04-28 Uop Two-stage process for producing diisopropyl ether using catalytic distillation
EP0733615A1 (en) * 1995-03-20 1996-09-25 Uop Process for producing diisopropyl ether

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