CN101445448A - A energy optimize utilizing process of acroleic acid device reaction unit - Google Patents
A energy optimize utilizing process of acroleic acid device reaction unit Download PDFInfo
- Publication number
- CN101445448A CN101445448A CNA2009100664088A CN200910066408A CN101445448A CN 101445448 A CN101445448 A CN 101445448A CN A2009100664088 A CNA2009100664088 A CN A2009100664088A CN 200910066408 A CN200910066408 A CN 200910066408A CN 101445448 A CN101445448 A CN 101445448A
- Authority
- CN
- China
- Prior art keywords
- steam
- tail gas
- heat
- reactor
- flash tank
- 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.)
- Granted
Links
Images
Landscapes
- Engine Equipment That Uses Special Cycles (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention discloses an energy optimize utilizing process of acroleic acid device reaction unit. Heat of reaction generated by reactor R-1, R-2 is carried out by a heat carrier, heats cooling water through a cooler and sends to a flash tank, characterized in that steam after flash evaporation through the flash tank transmitted into overheater for excessive heating and steam after excessive heating used to drive air compressing engine of the device for turbine, wherein the overheater is provided behind a knockout tower tail gas incineration furnace and overheats steam by tail gas burning heat. The beneficial effect of the invention is that burning of knockout tower tail gas decreases pollution to natural environment; tail gas can be recycled as valuable fuel; generated overheated steam can be used to drive air compressing engine for turbine, hence no need to build boiler and add overheater, therefore building cost of projects can be reduced, device operating cost can be lowed down, and the economic and social benefit are both significant.
Description
Technical field
The present invention relates to a kind of organic chemicals vinylformic acid production technique.
Background technology
Propylene second oxidation method is produced vinylformic acid, is a thermopositive reaction.Reaction is finished in two steps.The first step propylene oxidation generates propenal, and second step further was oxidized to vinylformic acid with propenal.Its reaction formula is as follows:
CH
2＝CH-CH
3+O
2→CH
2＝CH-CHO+H
2O+334.88kJ
CH
2＝CH-CHO+1/2O
2→CH
2＝CHCOOH+251.16kJ
From above-mentioned reaction formula as can be seen, react by propylene and airborne oxygen, the heat that the vinylformic acid of every generation 1mol will be emitted 586.04kJ, these heats are removed by molten heat transfer salt, by the saturation steam of water cooler generation certain pressure, send into steam pipe system.Simultaneously, the waste gas that reaction member produces need enter the catalytic burning system and carry out the catalytic burning processing, can discharge a large amount of heats, can not utilize, and causes energy dissipation, the expense when increasing the waste gas cooling again.Reaction member needs superheated vapour to drive with the turbine of air compressor, need mend not superheated vapour.Existing plant energy consumption height, the wasting of resources, contaminate environment, thereby the overall efficiency of reduction device.
Summary of the invention
The objective of the invention is to overcome the deficiency of prior art, a kind of energy-optimised technology of utilizing of acroleic acid device reaction unit is provided.
In the vinylformic acid production process, in the first reactor R-1, propylene is oxidized to propenal selectively, and the minor amounts of acrolein deep oxidation becomes vinylformic acid.The heat that reaction generates is shifted out by the inorganic salt thermal barrier (hereinafter to be referred as HTS) that is circulated in the reactor shell side, and this heat produces 1.5MPaG steam by E-3 and E-4 (R-1 the one HTS water cooler and R-1 the 2nd HTS water cooler) and enters high pressure steam jar D-4 afterwards.
In the second reactor R-2, acrolein oxidation becomes vinylformic acid, and the heat that reaction generates is shifted out by the HTS that is circulated in the reactor shell side, and this heat produces 1.5MPaG steam by E-5 (the HTS water cooler of R-2) and enters flash tank D-4 afterwards.
In flash tank D-4, produce the saturation steam of constant voltage.
The solution of the present invention is: the saturation steam that reaction member high pressure steam jar D-4 is produced is sent into catalytic burning unit superheater E-7 and is carried out overheatedly, and its temperature of superheat can be required by the turbine of compressor decide.
The heat that reactor produces can generate the steam of 1.5-2.0MPaG in E-3, E-4 and E-5.The steam that produces is sent into the further flash distillation of flash tank D-4, can generate the saturation steam of 1.5-2.0MPaG after the pressurize.
A kind of energy-optimised technology of utilizing of acroleic acid device reaction unit, the reaction heat that the first reactor R-1 generates is shifted out by the thermal barrier that is circulated in the reactor shell side, through water cooler E-3, E-4, with the water coolant heating and deliver to flash tank D-4; The reaction heat that the second reactor R-2 generates, shift out by the thermal barrier that is circulated in the reactor shell side, through water cooler E-5, with water coolant heating and deliver to flash tank D-4, flash tank D-4 flash distillation gets steam 1.5MPa～2.0MPa, it is characterized in that, steam after this flash distillation is sent into superheater E-7, it is overheated to carry out, its pressure 1.5～2.0MPa, 300～320 ℃ of overheated back vapor temperatures, the steam after overheated is used as the power that compressor KT-1 drives turbine, and the exhaust temperature of incinerator R-4 is reduced to 400～450 ℃ from 500～550 ℃.Superheater E-7 is located at after knockout tower C-1 cat head emits tail gas burning furnace R-4, burns heat with its tail gas and is used for steam superheating.
Remarkable benefit of the present invention, the reactor outlet temperature of catalytic burning system can reach about 550 ℃, produce superheated vapour through waste heat boiler after, 1, the temperature of waste gas can drop to about 450 ℃. reduced the load of exhaust gas cooler and the exhaust temperature of cleaning of off-gas.2, the superheated vapour that produces through waste heat boiler can reduce the energy consumption of device continuously for the air compressor turbine use of reactive system.
Adopt the present invention also can play the effect of flexible operating at the driving initial stage of device, the driving initial stage can be introduced external source of the gas, when the device load reaches 100% the unitary superheated vapour of catalytic burning is switched to compressor turbine.
If there is not enough steam to use outside the device battery limit (BL), can before driving, reactive system start the catalytic burning system for driving.In the stove that goes into operation of catalytic burning system, add fuel gas, the temperature of control catalytic burning reactor, liberated heat is produced 1.5-2.0MPaG by waste heat boiler saturation steam uses for driving initial stage compressor turbine.When the device load reaches 70%, close fuel gas charging valve gradually.
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 utility model is made detailed description further.
Certain produces 80000 tons of acroleic acid devices per year, and the reactive system liberated heat is 29943kW/h, and by E-3, it is 25.787t/h that E-4, E-105 produce the 1.5MPaG saturation steam respectively, 2.973t/h, 14.192t/h.The catalytic burning system will produce the heat of 29943kW/h, and it is 8.69t/h that E-6 produces the 1.5MPaG saturation steam.KT-1 consumes 1.5MPaG superheated vapour 45t/h.Produce the 0.3MPaG steam of 44.37t/h.After the invention process, can utilize the heat of the used heat 29943kW/h of catalytic burning system, compressor turbine need not external steam, needn't establish steam boiler, steam superheating apparatus in addition, reduces initial cost and working cost.
When the initial stage of driving, the turbine of compressor drives can dual mode.First kind of mode, the fuel gas of the certain calorific value of feeding in the stove that goes into operation of catalytic burning system when producing 1.5MPaG constant voltage saturation steam 8.69t/h, is introduced KT-1 with this steam earlier, when load reaches 70%, the inlet valve of fuel shutoff gas.At this moment, the steam that reactor is produced switches in the overheated steaming device of catalytic burning.The superheated vapour that produces is fed among the KT-1.KT-1 produces the 0.3MPaG saturation steam simultaneously.
The second way is: the driving initial stage is introduced the 1.5MPaG saturation steam from outside ductwork, uses for KT-1.When load reached 70%, it is stable that reactor produces steam, and the high pressure steam that D-4 is produced switches to the superheated vapour that produces in the vapor superheater under this pressure, uses for KT-1.
The invention has the advantages that the cat head of knockout tower C-1 is emitted tail gas after incinerator R-4 burns, If it is overheated that the steam that superheater E-7 comes out to D-4 carries out, KT-1 drives for this device air compressor The usefulness of turbine, tail gas burns, and reduces the pollution to atmosphere, and its tail gas acts as a fuel and recycles, Heat is used for heating steam, and this superheated steam is sent into the turbine of KT-1, thereby needn't build boiler for this reason again, Set up filter apparatus and can reduce construction costs, reduce the operating cost of device, its economic and society's effect Yidu is significant.
Claims (2)
1, the energy-optimised technology of utilizing of acroleic acid device reaction unit, the reaction heat that the first reactor R-1 generates is shifted out by the thermal barrier that is circulated in the reactor shell side, through water cooler E-3, E-4, with the water coolant heating and deliver to flash tank D-4; The reaction heat that the second reactor R-2 generates, shift out by the thermal barrier that is circulated in the reactor shell side, through water cooler E-5, with water coolant heating and deliver to flash tank D-4, flash tank D-4 flash distillation gets steam 1.5MPa～2.0MPa, it is characterized in that, steam after this flash distillation is sent into superheater E-7, it is overheated to carry out, its pressure 1.5～2.0MPa, 300～320 ℃ of overheated back vapor temperatures, the steam after overheated is used as the power that compressor KT-1 drives turbine, and the exhaust temperature of incinerator R-4 is reduced to 400～450 ℃ from 500～550 ℃.
According to the energy-optimised technology of utilizing of the described acroleic acid device reaction unit of claim 1, it is characterized in that 2, described superheater E-7 is located at after knockout tower C-1 cat head emits tail gas burning furnace R-4, burn heat with its tail gas and be used for steam superheating.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100664088A CN101445448B (en) | 2009-01-01 | 2009-01-01 | A energy optimize utilizing process of acroleic acid device reaction unit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100664088A CN101445448B (en) | 2009-01-01 | 2009-01-01 | A energy optimize utilizing process of acroleic acid device reaction unit |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101445448A true CN101445448A (en) | 2009-06-03 |
| CN101445448B CN101445448B (en) | 2011-10-26 |
Family
ID=40741374
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009100664088A Active CN101445448B (en) | 2009-01-01 | 2009-01-01 | A energy optimize utilizing process of acroleic acid device reaction unit |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101445448B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102874999A (en) * | 2011-07-12 | 2013-01-16 | 北大工学院绍兴技术研究院 | Sludge drying system utilizing waste heat |
| CN110981708A (en) * | 2019-12-30 | 2020-04-10 | 宁夏荆洪生物科技有限公司 | High-efficient pollution-free acrolein production system |
| CN111018226A (en) * | 2019-12-30 | 2020-04-17 | 宁夏荆洪生物科技有限公司 | Acrolein by-product acid water treatment system |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2436818C3 (en) * | 1974-07-31 | 1985-05-09 | Basf Ag, 6700 Ludwigshafen | Process for the production of acrylic acid by oxidation of propylene with gases containing oxygen in two separate oxidation stages |
| JP4056429B2 (en) * | 2003-06-05 | 2008-03-05 | 株式会社日本触媒 | Method for producing (meth) acrylic acid |
| CN101260032B (en) * | 2008-01-27 | 2010-09-29 | 中国石油集团工程设计有限责任公司东北分公司 | Modified technique for preparing acrylic acid by propylene two-step oxygenation method |
-
2009
- 2009-01-01 CN CN2009100664088A patent/CN101445448B/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102874999A (en) * | 2011-07-12 | 2013-01-16 | 北大工学院绍兴技术研究院 | Sludge drying system utilizing waste heat |
| CN110981708A (en) * | 2019-12-30 | 2020-04-10 | 宁夏荆洪生物科技有限公司 | High-efficient pollution-free acrolein production system |
| CN111018226A (en) * | 2019-12-30 | 2020-04-17 | 宁夏荆洪生物科技有限公司 | Acrolein by-product acid water treatment system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101445448B (en) | 2011-10-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100338424C (en) | Generating set system of simple low temperature waste heat from large size cement manufacture line in dry method, and technical process | |
| CN201218660Y (en) | Power generation apparatus by waste heat of sintering production | |
| CN101532402A (en) | Dual-circulation screw expansion motor system | |
| CN101445448B (en) | A energy optimize utilizing process of acroleic acid device reaction unit | |
| CN105737123A (en) | Blast furnace gas distributed energy system | |
| CN113028376A (en) | Ammonia chemical looping combustion power generation system and method | |
| CN101706215A (en) | Method and device for double-source power cogeneration with sintering waste heat | |
| CN203549758U (en) | Carbon calciner waste heat boiler | |
| CN201386572Y (en) | Bi-circulating screw expansion power machine system utilizing working medium with low boiling point | |
| CN202350552U (en) | Generating device using residual heat of magnesium oxide powder of magnesium oxide calcination rotary kiln | |
| CN202350551U (en) | Generating device using residual heat of smoke of magnesium oxide calcination rotary kiln | |
| CN201589537U (en) | Device utilizing deaerating feed to heat condensed water in cement kiln afterheat generation | |
| CN201978726U (en) | Self-heating temperature-raising type formaldehyde reactor | |
| JP4823998B2 (en) | Waste power generation method | |
| CN203050821U (en) | Methanol reaction heat recovery system | |
| CN203657509U (en) | Submerged arc furnace smoke waste-heat utilization system | |
| CN201991651U (en) | Pure liquid oxygen fuel oil power generator | |
| CN103673644A (en) | Waste heat utilizing system of submerged-arc furnace | |
| CN221397816U (en) | Industrial steam device for biomass gasification gas boiler production | |
| RU2787627C1 (en) | Method for operation of a combined gas and steam unit of a power plant | |
| CN102211884B (en) | High-efficiency, energy-saving and environment-friendly lime manufacturing unit | |
| CN103383202A (en) | Organic Rankine waste heat generating and dust removing method utilizing flue gas from interior of electric furnace | |
| BE1021414B1 (en) | EXHAUST GAS TREATMENT DEVICE AND METHOD FOR COOLING AND NEUTRALIZING EXHAUST GAS OF A COMBUSTION DEVICE | |
| CN202613403U (en) | Sintering waste heat boiler | |
| CN212406827U (en) | Steam extraction waste heat utilization system for deep peak regulation |
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 | ||
| C56 | Change in the name or address of the patentee | ||
| CP03 | Change of name, title or address |
Address after: Changyi District of Jilin city of Jilin Province on the 132002 road at the eastern end of Lake Jilin Trade 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: PetroChina Northeast Refining & Chemical Engineering Co., Ltd. Jilin Design Institute |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20200929 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: Changyi District of Jilin city of Jilin Province on the 132002 road at the eastern end of Lake Jilin Trade Building Patentee before: JILIN DESIGNING INSTITUTE OF CNPC NORTHEAST REFINING & CHEMICAL ENGINEERING Co.,Ltd. |
|
| TR01 | Transfer of patent right |