CN101260033B - Fresh air temperature control system for preparing acrylic acid by propylene two-step oxygenation method - Google Patents
Fresh air temperature control system for preparing acrylic acid by propylene two-step oxygenation method Download PDFInfo
- Publication number
- CN101260033B CN101260033B CN2008100503556A CN200810050355A CN101260033B CN 101260033 B CN101260033 B CN 101260033B CN 2008100503556 A CN2008100503556 A CN 2008100503556A CN 200810050355 A CN200810050355 A CN 200810050355A CN 101260033 B CN101260033 B CN 101260033B
- Authority
- CN
- China
- Prior art keywords
- temperature
- propylene
- reactor
- air
- fresh air
- 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.)
- Active
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a fresh air temperature control system for acrylic acid preparation through a propylene two-step oxygen-adding method, which is characterized in that: a TRC-1001 thermocouple is arranged on a pipeline in front of a compressed air inlet premixer; the invention is provided with a temperature transmitter; the temperature transmitter outputs signals entering a DCS system of a device; DCS output signals of the invention control the class of electric heater of an air preheater; the temperature in front of the compressed air inlet premixer is controlled to be between 160 DEG C and 170 DEG C. Cold areas are great in the changes of atmospheric environmental temperature at four seasons and are great even in temperature difference of daytime and nighttime. The invention has the advantages that: the fresh air temperature control system can ensure that the feed temperature of fresh air is controlled in a permissible operating temperature range of catalyst performance, guarantee stable temperature of mixed gas, save the steam amount of the device, reduce heat consumption and avoid the interference to device operation caused by the changes of environmental temperature, soas to improve propylene conversion rate as well as acrylic acid yield and reduce production cost.
Description
Technical field
The present invention relates to the automatic control system in a kind of vinylformic acid production.
Technical background
Propylene two-step oxygenation legal system vinylformic acid is to carry out under the condition that oxide catalyst exists, and the first step wherein is that propylene oxidation generates propenal, and second step was that the further oxidation of propenal is generated vinylformic acid, and its reaction equation is as follows:
CH
2＝CH-CH
3+O
2→CH
2＝CH-CHO+H
2O
CH
2＝CH-CHO+1/2O
2→CH
2＝CH-COOH
Fresh air provides oxygen to participate in chemical reaction, and in the vinylformic acid oxidizing reaction, consumption of fresh air is big, uses the oxide catalyst of different manufacturers for the fresh air feeding temperature different requirements to be arranged.With 80,000 tons of/year acroleic acid devices is example, certain producer's oxide catalyst performance requriements first oxidation reactor inlet mixed gas temperature is 150 ℃～200 ℃ scopes, the fresh air feeding temperature is controlled at more than 160 ℃ before promptly requiring to mix, most devices are provided with airheater between the entry mixers M-1002 and the first reactor R-1001, energy consumption is bigger, and the interference that the device operation is constantly changed by envrionment temperature, the feasible mixed gas temperature instability that enters the first reactor R-1001, thereby influence catalyst performance, influence the vinylformic acid yield.
Summary of the invention
The objective of the invention is to overcome the deficiency of prior art, a kind of new acrylic acid fresh air temperature control system of propylene two-step oxygenation legal system is provided.
The acrylic acid fresh air temperature control system of propylene two-step oxygenation legal system, fresh air, steam, recycled offgas advance premixer M-1001 in the acrylic acid propylene oxidation unit of propylene two-step oxygenation legal system, enter mixing tank M-1002 with propylene again, carry out thorough mixing, charging as the first reactor R-1001, under the catalyzer existence condition, propylene and airborne oxygen carry out chemical reaction in the first reactor R-1001, generate propenal and a small amount of vinylformic acid; Be provided with air preheater H-1001 in air compressor K-1001 outlet, H-1001 is the first oxidation reactor R-1001 attendant equipment, and air preheater H-1001 Outlet Gas Temperature is adjusted variation with device operating environment temperature variation.The invention is characterized in: the thermopair that is provided with TRC-1001 on the pipeline before pressurized air advances premixer M-1001, is furnished with temperature transmitter, the DCS system of temperature transmitter output signal motion device, the electric heater group of its DCS output signal control air preheater H-1001, control air are advanced the preceding temperature of premixer M-1001 between 160 ℃～170 ℃; Or establish simultaneously the thermopair of TRC-1002 on the pipeline before gas mixture enters the first reactor R-1001, be equipped with temperature transmitter, the DCS system of its output signal motion device, its DCS system output signal is made the given signal of TRC-1001 regulation system, constitute cascade control system, advance the temperature given value of premixer M-1001 with the mixed gas temperature signal correction air that enters the first reactor R-1001.
Big in NORTHWEST CHINA, North China, the Northeast's atmospheric environment temperature variation, throughout the year between so, day and night, the temperature difference was also bigger.The invention has the advantages that; be provided with the fresh air temperature control system that enters the first reactor R-1001; the fresh air feeding temperature is controlled in the operating temperature range of catalyst performance permission; to guarantee the mixed gas temperature-stable; the economizer steam consumption reduces heat energy consumption, has avoided again because of the interference of variation of ambient temperature to the oxide catalyst performance; to improve propylene conversion, improve acrylic acid yield.
Description of drawings
Fig. 1 is the concise and to the point process flow sheet of the present invention.
Embodiment
Below in conjunction with specific examples the present invention is made detailed description further.
Present existing same device is to be provided with airheater between the entry mixers M-1001 and the first reactor R-1001, with low pressure steam as thermal source, and the present invention cancels it, minimizing equipment, reduce the plant construction expense, reducing energy consumption, reduce production costs, adopt the first oxidation reactor R-1001 to assist carrying equipment---air preheater H-1001 electric heater carries out the first reactor inlet mixed gas temperature regulation; Be provided with the thermopair of TRC-1001 on the pipeline before pressurized air advances premixer M-1001, is furnished with temperature transmitter, the DCS system of temperature transmitter output signal motion device, the electric heater group of its DCS output signal control air preheater H-1001, control air are advanced the preceding temperature of premixer M-1001 between 160 ℃～170 ℃; Or establish simultaneously the thermopair of TRC-1002 on the pipeline before gas mixture enters the first reactor R-1001, be equipped with temperature transmitter, the DCS system of its output signal motion device, its DCS system output signal is made the given signal of TRC-1001 regulation system, constitute cascade control system, advance the temperature given value of premixer M-1001 with the mixed gas temperature signal correction air that enters the first reactor R-1001.
At northern somewhere 80,000 tons of/year acroleic acid device local environments temperature extreme minimum temperature-20 ℃, 30 ℃ of the high ambient temperatures of the hottest monthly average, year-round average temperature is 10 ℃.Its oxide catalyst supplier requires the first oxidation reactor gasinlet temperature need be controlled between 150 ℃～200 ℃, air compressor is the secondary compression in the oxidizing reaction operational path, and its temperature out changes between 120 ℃～175 ℃ with variation of ambient temperature.Usually the air compressor of secondary compression is equipped with interstage cooler, comparable device operation practical situation, for guaranteeing that this installs the first reactor R-1001 gasinlet temperature and reaches catalyzer supply merchant operational requirement, cancellation air compressor inter-stage water cooler, improve the compressor outlet air themperature, thereby improve the R-1001 gasinlet temperature so that it reaches requirement; Simultaneously, do not set up the one-time investment that airheater reduces equipment.
Consider that according to this device local environment temperature variations following countermeasure adjusts the heating of H-1001 electric heater and organize to satisfy the first reactor R-1001 gasinlet temperature and reach the catalyzer operational requirement.
1. when envrionment temperature reached extreme minimum temperature-20 ℃, the air compressor temperature out was 120 ℃, and can control opening electric heater H-1001 this moment by DCS.H-1001 has many group an electric heating element, opens one group and can make into that the first reactor R-1001 air themperature raises 15 ℃, opens for three groups to make air themperature be increased to 165 ℃ from 120 ℃, and such first reactor R-1001 inlet air temperature can reach 150 ℃.
2. when 10 ℃ of envrionment temperatures, the air compressor temperature out is 155 ℃, does not open electric heater H-1001, and the first reactor R-1001 inlet air temperature is 140 ℃; Drive one group of electric heater, air themperature is upgraded to 170 ℃, and the first reactor R-1001 inlet air temperature is 150 ℃.
3. when envrionment temperature was 20 ℃, the air compressor temperature out was 166 ℃, and the first reactor R-1001 inlet air temperature is 150 ℃, can not drive well heater.
4. when 30 ℃ of extremely high ambient temperatures, the air compressor temperature out is 175 ℃, and the first reactor R-1001 inlet air temperature is 155 ℃, can not drive well heater.
According to The above results as can be seen, when envrionment temperature 〉=20 ℃, first reactor R-1001 inlet mixed gas temperature can reach 150 ℃～200 ℃, does not need to open H-1001; When envrionment temperature during at 19 ℃～10 ℃, open one group of electric heater of H-1001 by DCS control, can satisfy first reactor R-1001 inlet mixed gas temperature requirement; When envrionment temperature during at 10 ℃～-10 ℃, open two groups of electric heaters of H-1001 by DCS control, can satisfy first reactor R-1001 inlet mixed gas temperature requirement; When envrionment temperature during at-10 ℃～-20 ℃, open three groups of electric heaters of H-1001 by DCS control, can satisfy first reactor R-1001 inlet mixed gas temperature requirement.According to when the ground temperature situation, when envrionment temperature is low, open H-1001, three groups of electric heaters of H-1001 are in out two substantially and are equipped with or two open one and be equipped with situation, three groups of electric heaters need time of opening simultaneously the operating period in 1 year shared probability very short.Therefore in the H-1001 working order, its three groups of electric heaters have one group or two groups to be in stand-by state all the time, can guarantee stable, the normal operation of H-1001.
If above-mentioned example device is built the extreme minimum temperature of place, ground envrionment temperature between-40 ℃～-20 ℃ scopes, can be according to practical situation, increase H-1001 electric heater group number (or improving single group electric heater capacity), make it reach the requirement temperature to satisfy heating air compressor exit gas.
In the firm start-up of device, the operator of device can organize the adjusting of carrying out the first reactor inlet gas temperature by the heating of DCS hand control switch H-1001 electric heater; After device was driven for some time, DCS control H-1001 mode can change DCS into by the manual control of operator and control automatically, makes device operation safe, reliable like this, has also saved device post personnel simultaneously and has dropped into, the raising overall efficiency.
Claims (2)
1. the temperature controlling system of propylene two-step oxygenation legal system vinylformic acid fresh air, fresh air, steam, recycled offgas advance premixer (M-1001) in the acrylic acid propylene oxidation unit of propylene two-step oxygenation legal system, enter mixing tank (M-1002) with propylene again, carry out thorough mixing, charging as first reactor (R-1001), under the condition that catalyzer exists, propylene and airborne oxygen carry out chemical reaction in first reactor (R-1001), generate propenal and a small amount of vinylformic acid; Be provided with air preheater (H-1001) in air compressor (K-1001) outlet, (H-1001) be first oxidation reactor (R-1001) attendant equipment, air preheater (H-1001) Outlet Gas Temperature is adjusted variation with device operating environment temperature variation, it is characterized in that: advance the thermopair that is provided with TRC-1001 on the preceding pipeline of premixer (M-1001) at pressurized air, is furnished with temperature transmitter, the DCS system of temperature transmitter output signal motion device, the electric heater group of its DCS output signal control air preheater (H-1001), control air are advanced the preceding temperature of premixer (M-1001) between 160 ℃ ~ 170 ℃.
2. according to the acrylic acid fresh air temperature control system of the described propylene two-step oxygenation legal system of claim 1, it is characterized in that, enter the thermopair of establishing TRC-1002 on the preceding pipeline of first reactor (R-1001) at mixing tank, be equipped with temperature transmitter, the DCS system of its output signal motion device, its DCS system output signal is made the given signal of TRC-1001 regulation system, constitute cascade control system, advance the temperature given value of premixer (M-1001) with the mixed gas temperature signal correction air that enters first reactor (R-1001).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008100503556A CN101260033B (en) | 2008-01-27 | 2008-01-27 | Fresh air temperature control system for preparing acrylic acid by propylene two-step oxygenation method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008100503556A CN101260033B (en) | 2008-01-27 | 2008-01-27 | Fresh air temperature control system for preparing acrylic acid by propylene two-step oxygenation method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101260033A CN101260033A (en) | 2008-09-10 |
| CN101260033B true CN101260033B (en) | 2010-09-22 |
Family
ID=39960770
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2008100503556A Active CN101260033B (en) | 2008-01-27 | 2008-01-27 | Fresh air temperature control system for preparing acrylic acid by propylene two-step oxygenation method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101260033B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101584969B (en) * | 2009-06-23 | 2012-08-29 | 中石油东北炼化工程有限公司吉林设计院 | Mixer for preparing acrylic acid through propylene two-step oxygenation method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1105352A (en) * | 1994-11-23 | 1995-07-19 | 大庆石油学院 | Process for producing propenoic acid by homogenization, oxydation and dehydrogenation of propane, and propene oxydation, and apparatus thereof |
| US6281384B1 (en) * | 1998-06-26 | 2001-08-28 | E. I. Du Pont Nemours And Company | Vapor phase catalytic oxidation of propylene to acrylic acid |
| CN1697689A (en) * | 2004-05-27 | 2005-11-16 | 三菱化学株式会社 | Reactor, reactor control system, and catalytic gas phase oxidation reaction method |
| CN1944377A (en) * | 2006-10-27 | 2007-04-11 | 清华大学 | Multistage fluidized bed reactor for preparing propenoic acid from propene oxidation and preparing method |
| CN201172642Y (en) * | 2008-01-27 | 2008-12-31 | 中国石油集团工程设计有限责任公司东北分公司 | Air control system in production device of acrylic acid |
-
2008
- 2008-01-27 CN CN2008100503556A patent/CN101260033B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1105352A (en) * | 1994-11-23 | 1995-07-19 | 大庆石油学院 | Process for producing propenoic acid by homogenization, oxydation and dehydrogenation of propane, and propene oxydation, and apparatus thereof |
| US6281384B1 (en) * | 1998-06-26 | 2001-08-28 | E. I. Du Pont Nemours And Company | Vapor phase catalytic oxidation of propylene to acrylic acid |
| CN1697689A (en) * | 2004-05-27 | 2005-11-16 | 三菱化学株式会社 | Reactor, reactor control system, and catalytic gas phase oxidation reaction method |
| CN1944377A (en) * | 2006-10-27 | 2007-04-11 | 清华大学 | Multistage fluidized bed reactor for preparing propenoic acid from propene oxidation and preparing method |
| CN201172642Y (en) * | 2008-01-27 | 2008-12-31 | 中国石油集团工程设计有限责任公司东北分公司 | Air control system in production device of acrylic acid |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101260033A (en) | 2008-09-10 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2003061031A3 (en) | Method and apparatus for preventing water in fuel cell power plants from freezing during storage | |
| CN105112100A (en) | Continuous production technique of chlorinated paraffin | |
| CN109860660A (en) | A kind of high-performance solid oxide fuel battery system | |
| CN102511101B (en) | Fuel cell device | |
| CN201172642Y (en) | Air control system in production device of acrylic acid | |
| CN101260033B (en) | Fresh air temperature control system for preparing acrylic acid by propylene two-step oxygenation method | |
| CN111883805B (en) | Small-size methyl alcohol reforming hydrogen plant system based on tail gas waste heat utilization | |
| CN102731320B (en) | Method for absorbing nitrogen oxide tail gas and generating by-product p-phenylenediamine by using aniline | |
| CN105992838A (en) | A system for utilizing excess heat for carrying out electrochemical reactions | |
| JPH02163007A (en) | Cultivation apparatus utilizing fuel battery | |
| CN204454653U (en) | The synthesizer of Tai-Ace S 150 | |
| CN103506060B (en) | Energy-saving type oxyanthraquinone production device | |
| CN202938632U (en) | Energy-saving core rod preheating furnace heat-supply device | |
| CN105502299A (en) | Radio-frequency radiation production line for quickly preparing aerogel powder | |
| CN103508457A (en) | Production device provided with polycrystalline silicon decomposing furnaces and operation method for production device | |
| CN210855262U (en) | Methanol reforming hydrogen production system | |
| CN114291800A (en) | Preparation method of neutral lithium phosphate | |
| CN211601193U (en) | Novel forming chamber cooling and air waste heat recovery replaces electric heating system | |
| CN108649248B (en) | Hydrogen recovery system of cold rolling treatment line annealing furnace | |
| CN112113210A (en) | Energy-saving catalytic oxidation heating equipment for cloth setting machine | |
| CN203513270U (en) | Improved methanation warming device for synthesizing ammonia | |
| CN102391082A (en) | Method and device for heat exchange of methanol in production of formaldehyde | |
| CN219150112U (en) | Quick cooling device of strong exothermic reaction kettle | |
| CN213777702U (en) | Catalytic oxidation heat supply equipment for cloth setting machine | |
| CN204385106U (en) | A kind of novel barkite cools back receiving apparatus |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20161123 Address after: 132002 Jilin, Changyi District, Tung Tam Road, grand Peng Peng building Patentee after: Jilin Design Institute of Northeast Refining & Chemical Engineering Co., Ltd., CNPC Address before: Changyi District of Jilin city of Jilin Province on the 132022 road at the eastern end of Lake Jilin Trade Building Patentee before: Dongbei Branch Co., China Petroleum Group Engineering Designing Co., Ltd. |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20200930 Address after: 132002 3-6 and 9-13 floors of Block A, Jihua Economic and Trade Center, Tongtan Road, Changyi District, Jilin Province Patentee after: PetroChina Jilin Chemical Engineering Co.,Ltd. Address before: 132002 Jilin, Changyi District, Tung Tam Road, grand Peng Peng building Patentee before: JILIN DESIGNING INSTITUTE OF CNPC NORTHEAST REFINING & CHEMICAL ENGINEERING Co.,Ltd. |
|
| TR01 | Transfer of patent right |