AU2018101974A4 - Extractant 2-methyl-2-methoxypropane production plant - Google Patents
Extractant 2-methyl-2-methoxypropane production plant Download PDFInfo
- Publication number
- AU2018101974A4 AU2018101974A4 AU2018101974A AU2018101974A AU2018101974A4 AU 2018101974 A4 AU2018101974 A4 AU 2018101974A4 AU 2018101974 A AU2018101974 A AU 2018101974A AU 2018101974 A AU2018101974 A AU 2018101974A AU 2018101974 A4 AU2018101974 A4 AU 2018101974A4
- Authority
- AU
- Australia
- Prior art keywords
- methyl
- methoxypropane
- extractant
- bed reactor
- fixed bed
- Prior art date
- Legal status (The legal status 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 status listed.)
- Ceased
Links
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
- C07C41/05—Preparation of ethers by addition of compounds to unsaturated compounds
- C07C41/06—Preparation of ethers by addition of compounds to unsaturated compounds by addition of organic compounds only
-
- 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
- C07C41/34—Separation; Purification; Stabilisation; Use of additives
- C07C41/40—Separation; Purification; Stabilisation; Use of additives by change of physical state, e.g. by crystallisation
- C07C41/42—Separation; Purification; Stabilisation; Use of additives by change of physical state, e.g. by crystallisation by distillation
Abstract
Extractant 2-methyl-2-methoxypropane production plant Abstract 5 Extractant 2-methyl-2-methoxypropane production plant, including: tank (F101, F102), tubular fixed bed reactor (D101), pump (J101, J102), rectifying column (E101), separator (LIO); among them, pump (JIO) is connected respectively to tank (FlO) and tubular fixed bed reactor (D101), separator (LIO) is connected respectively to tubular fixed bed reactor (DI01) and rectifying column (E10); among them, nominal 10 volume of tank (FlO) is 6.2-6.5 in3 . Figure 1 eating steam from the heating station fractions' j n101 L fM th ano F102tes Steam condensate back to the heating station Figure I
Description
Extractant 2-methyl-2-methoxypropane production plant
FIELD OF THE INVENTION
The present invention relates to a kind of pharmaceutical synthesis plant, more particularly, relates to extractant 2-methyl-2-methoxypropane production plant.
GENERAL BACKGROUND
2-methyl-2-methoxypropane is mainly used as gasoline additive to increase the octane number. It also can be cracked to obtain isobutylene. As a gasoline additive, it has excellent antiknock properties. It has good miscibility with gasoline, less water absorption, no pollution to the environment, can improve the gasoline cold start characteristics and acceleration performance, without adverse effects on the gas resistance. Although methyl tert-butyl ether has a low calorific value, driving tests show that the use of gasoline containing 10% MTBE can reduce fuel consumption by 7% and significantly reduce the emission of lead, CO and especially carcinogenic PAHs. As an organic synthesis raw material, it can make high purity isobutene. It can also be used for the production of 2-methacrolein, methacrylic acid and isoprene, etc., and can also be used as analytical solvent, extractant. Most of the existing production plant processes are complex. Thus, as an extractant, the advantages and disadvantages of production equipment of 2-methyl-2-methoxypropane have a great economic significant for improving product quality and reducing the by-product contents.
SUMMARY
The purpose of the present invention is to provide extractant 2-methyl-2-methoxypropane production plant, including: tank (F101, Fl02), tubular fixed bed reactor (D101), pump (J101, J102), rectifying column (E101), separator (LI01); among them, pump (JI01) is connected respectively to tank (Fl01) and tubular fixed bed reactor (D101), separator (L101) is connected respectively to tubular fixed bed reactor (D101) and rectifying column (E101); among them, nominal volume of tank (F101) is 6.2-6.5 m3, heat pipe inside diameter of tubular fixed bed reactor (D101) is 0.016-0.018 m, inlet diameter of pump (JI 01) is 170-176 mm.
2018101974 05 Dec 2018
Extractant 2-methyl-2-methoxypropane production plant, the production process is: mixed isobutylene-containing C4 fraction and methanol, preheated to 40-46 °C, sent to 40-46 °C, used macroporous network of cation exchange resin as a catalyst, controlled the reaction temperature at 40-45 °C, used cooling water to control the 5 temperature, controlled the liquid phase velocity at 43-45 m3/h, used slightly excessive methanol. After the reaction is completed, separated the product through separator L101, separated the crude product of 99% purity, rectified the crude product in the rectifying column E101 for 2-3 h and obtained the finished product. The advantages of this invention are that the reaction time is reduced and the reaction rate 10 is improved.
DESCRIPTION OF THE DRAWINGS
Figure 1 is extractant 2-methyl-2-methoxypropane production plant.
Include: tank (F101, Fl02), tubular fixed bed reactor (D101), pump (JI01, J102), rectifying column (E101), separator (L101);
DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS
The following examples with reference to specific embodiments of the present invention are further illustrated:
Embodiment 1
Raw materials and dosages
| Methanol | Industrial grade | 800 | Isobutylene | Industrial grade | 1400 |
Extractant 2-methyl-2-methoxypropane production plant, including: tank (F101,
F102), tubular fixed bed reactor (D101), pump (JI01, J102), rectifying column (E101), separator (LI01); among them, pump (JI01) is connected respectively to tank (Fl01) and tubular fixed bed reactor (D101), separator (LI01) is connected respectively to tubular fixed bed reactor (D101) and rectifying column (E101); among them, nominal volume of tank (F101) is 6.2 m3, heat pipe inside diameter of tubular fixed bed reactor (D101) is 0.016 m, inlet diameter of pump (J101) is 170 mm.
Extractant 2-methyl-2-methoxypropane production plant, the production process
2018101974 05 Dec 2018 is: mixed isobutylene-containing C4 fraction and methanol, preheated to 40 °C, sent to °C, used macroporous network of cation exchange resin as a catalyst, controlled the reaction temperature at 40 °C, used cooling water to control the temperature, controlled the liquid phase velocity at 43 m3/h, used slightly excessive methanol.
After the reaction is completed, separated the product through separator L101, separated the crude product of 99% purity, rectified the crude product in the rectifying column El01 for 2 h and obtained the finished product.
The qualities of the product are as follows:
| Exterior | Low viscosity, colorless liquid | /720 Relative density( 4 ) | 0.7405 |
| Freezing point | -108.6 °C | 2° Refractive index () | 1.3692 |
| Boiling point | 55 °C | ||
| Burning point | 459 °C |
Embodiment 2
Raw materials and dosages
| Methanol | Industrial grade | 900 | Isobutylene | Industrial grade | 1500 |
Extractant 2-methyl-2-methoxypropane production plant, including: tank (F101, F102), tubular fixed bed reactor (D101), pump (JI01, J102), rectifying column (E101), separator (LI01); among them, pump (JI01) is connected respectively to tank (Fl01) 15 and tubular fixed bed reactor (DI01), separator (LI01) is connected respectively to tubular fixed bed reactor (D101) and rectifying column (E101); among them, nominal volume of tank (F101) is 6.5 m3, heat pipe inside diameter of tubular fixed bed reactor (D101) is 0.018 m, inlet diameter of pump (J101) is 176 mm.
Extractant 2-methyl-2-methoxypropane production plant, the production process 20 is: mixed isobutylene-containing C4 fraction and methanol, preheated to 46 °C, sent to 46 °C, used macroporous network of cation exchange resin as a catalyst, controlled the reaction temperature at 45 °C, used cooling water to control the temperature, controlled the liquid phase velocity at 45 m3/h, used slightly excessive methanol.
After the reaction is completed, separated the product through separator L101, separated the crude product of 99% purity, rectified the crude product in the rectifying column El01 for 3 h and obtained the finished product.
2018101974 05 Dec 2018
The qualities of the product are as follows:
| Exterior | Low viscosity, colorless liquid | /720 Relative density( 4 ) | 0.7406 |
| Freezing point | -108.6 °C | 2° Refractive index () | 1.3693 |
| Boiling point | 56 °C | ||
| Burning point | 460 °C |
The embodiments of the present invention are merely preferred embodiments of the present invention, but the range of the present invention is not limited this, and any person who is familiar with those skilled in the arts, within the technical range of the present invention. It is intended that the technical solution and its inventive concept be replaced or modified equivalently with reference to the range of the 10 invention.
Claims (3)
- Claims1. Extractant 2-methyl-2-methoxypropane production plant, including: tank (F101, F102), tubular fixed bed reactor (D101), pump (J101, J102), rectifying column5 (El01), separator (LI01); among them, pump (JI01) is connected respectively to tank (Fl01) and tubular fixed bed reactor (DI01), separator (LI01) is connected respectively to tubular fixed bed reactor (DI01) and rectifying column (El01); among them, nominal volume of tank (F101) is 6.2-6.5 m3.
- 2. Extractant 2-methyl-2-methoxypropane production plant, according to claim 110 wherein heat pipe inside diameter of tubular fixed bed reactor (DI01) is 0.016-0.018m.
- 3. Extractant 2-methyl-2-methoxypropane production plant, according to claim 1 wherein inlet diameter of pump (J101) is 170-176 mm.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2017114474416 | 2017-12-27 | ||
| CN201711447441.6A CN108238858A (en) | 2017-12-27 | 2017-12-27 | The process units of extractant 2- methyl -2- methoxy propanes |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| AU2018101974A4 true AU2018101974A4 (en) | 2019-01-31 |
Family
ID=61158215
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU2018101974A Ceased AU2018101974A4 (en) | 2017-12-27 | 2018-12-05 | Extractant 2-methyl-2-methoxypropane production plant |
Country Status (3)
| Country | Link |
|---|---|
| CN (1) | CN108238858A (en) |
| AU (1) | AU2018101974A4 (en) |
| GB (1) | GB201722180D0 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114160050A (en) * | 2021-12-09 | 2022-03-11 | 万华化学(四川)有限公司 | Device system and method for continuously producing alkoxy propane |
-
2017
- 2017-12-27 CN CN201711447441.6A patent/CN108238858A/en not_active Withdrawn
- 2017-12-28 GB GBGB1722180.5A patent/GB201722180D0/en not_active Ceased
-
2018
- 2018-12-05 AU AU2018101974A patent/AU2018101974A4/en not_active Ceased
Also Published As
| Publication number | Publication date |
|---|---|
| GB201722180D0 (en) | 2018-02-14 |
| CN108238858A (en) | 2018-07-03 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| FGI | Letters patent sealed or granted (innovation patent) | ||
| MK22 | Patent ceased section 143a(d), or expired - non payment of renewal fee or expiry |