CN101644426A - Afterheat utilization method of reaction effluent in ethane production - Google Patents
Afterheat utilization method of reaction effluent in ethane production Download PDFInfo
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- CN101644426A CN101644426A CN200910034449A CN200910034449A CN101644426A CN 101644426 A CN101644426 A CN 101644426A CN 200910034449 A CN200910034449 A CN 200910034449A CN 200910034449 A CN200910034449 A CN 200910034449A CN 101644426 A CN101644426 A CN 101644426A
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Abstract
The invention relates to an afterheat utilization method, in particular to an afterheat utilization method of reaction effluent in ethane production, comprising the technical steps: firstly, a reaction effluent flows through a heat exchanger which is constantly introduced with boiler supply water, the boiler supply water is heated and flows into a boiler heat deaerator, at the same time, the reaction effluent is cooled to obtain a first condensate; and then, the first condensate flows into the other heat exchanger which is constantly introduced with circulating water to obtain a secondary condensate. The utilization method sufficiently uses the afterheat energy of the reaction effluent and reduces the vapor consumption of the boiler heat deaerator and the working load of a circulating water system, thereby effectively saving an energy source.
Description
Technical field
The present invention relates to a kind of UTILIZATION OF VESIDUAL HEAT IN method, particularly relate to reaction effluent afterheat utilization method in a kind of ethylene production.
Background technology
The steam that steam that adds in the ethylene production and reaction itself produces, through behind each procedure, it is 0.1～0.13Mpa that reaction effluent (being actually the mixture of various steams) temperature drops to 116～120 ℃, pressure.Because the temperature of reaction effluent is lower, in each unit operations of ethylene production, be difficult to be utilized, if but directly be disposed in the air, can cause environmental pollution again.
Press national regulation: evaporation capacity all must outfit boiler deoxidizing method device more than or equal to 95 ℃ hot-water boiler more than or equal to the steam boiler and the water temperature of 2 tphs.Deaerating plant is mainly used in dissolved oxygen and other incondensable gas of removing in the boiler feed water, to guarantee the quality of boiler feed water, makes boiler avoid corrosion.At present, employed boiler in the ethylene production mostly is furnished with the boiler heating power oxygen-eliminating device.Feed steam in this oxygen-eliminating device, boiler feedwater is heated to 104 ℃, 0.02MPa, make the partial pressure of gas phase oxygen be reduced to zero, the dissolved oxygen in the water also is reduced to zero, thereby removes the oxygen in the boiler feedwater.The mode of this deoxygenation exists steam and consumes high problem, has not only wasted the energy, and environment is caused negative effect.
At present, even at comparative maturity and in the ethylene unit of suitability for industrialized production, the waste heat of described reaction effluent is not fully utilized yet, and also need it be cooled off by the heat exchanger that continues to be connected with recirculated water.The air-cooled tower of recirculated water makes water continue and flow through heat exchanger (that is: in the air-cooled tower inflow heat exchanger of recirculated water feedwater self-circulating water of supercooling, the recirculated water backwater that flows out returns in the air-cooled tower of recirculated water and cools off) circularly in heat exchanger.The method has not only been wasted the waste heat energy of reaction effluent, and has increased the live load of circulation.
Summary of the invention
The technical problem to be solved in the present invention provides reaction effluent afterheat utilization method in a kind of ethylene production, adopt this method, made full use of the waste heat energy of reaction effluent, reduced the steam consumption of boiler heating power oxygen-eliminating device, reduce the live load of circulation, thereby effectively saved the energy.
For solving the problems of the technologies described above, the invention provides reaction effluent afterheat utilization method in a kind of ethylene production, processing step is: allow the reaction effluent heat exchanger that continues to be connected with boiler feedwater of flowing through earlier, make in boiler feedwater intensification and the inflow boiler heating power oxygen-eliminating device, meanwhile, make reaction effluent cooling and obtain condensate liquid one time, then, a condensate liquid gravity flow enters one and continues to be connected with in another heat exchanger of recirculated water, and obtains time condensation liquid.
After adopting this method, on the one hand, make the boiler feedwater water inlet can the contained waste heat of absorption reaction effluent and heat up, like this, the boiler feedwater water outlet flows in the boiler heating power oxygen-eliminating device and can be used, and has reduced the steam consumption of boiler heating power oxygen-eliminating device, the corresponding air demand that improves boiler; On the other hand, reaction effluent successively by a heat exchanger that continues to be connected with boiler feedwater, continue to be connected with another heat exchanger cooling of recirculated water, like this, the temperature of recirculated water backwater obviously reduces than background technology, reduced the live load of circulation, effectively reduce the power consumption of the air-cooled tower of recirculated water, saved the energy.
Therefore, the invention has the beneficial effects as follows: adopt this method, made full use of the waste heat energy of reaction effluent, reduced the steam consumption of boiler heating power oxygen-eliminating device, reduced the live load of circulation, thereby effectively saved the energy.
In addition, the present invention is simple and practical, investment is little.
According to test, the cost of steam consumption and fuel consumption effectively reduces in the ethylene production, and the total energy consumption of ethylene unit reduces about 50%.
The temperature of described reaction effluent is that 116～120 ℃, pressure are 0.1～0.13Mpa, and the temperature of a condensate liquid is 50～80 ℃, and the temperature of time condensation liquid is 20～30 ℃; The temperature of boiler feedwater water inlet is that 20～30 ℃, pressure are 0.3～0.4Mpa, and the temperature of boiler feedwater water outlet is that 90～100 ℃, pressure are 0.3～0.4Mpa; The temperature of recirculated water feedwater is 30～35 ℃, and the temperature of recirculated water backwater is 33～37 ℃.
Description of drawings
Accompanying drawing is the schematic diagram of this method specific embodiment.
The specific embodiment
Below further specify the present invention by embodiment and accompanying drawing thereof.But it is not a limitation of the invention.
Referring to accompanying drawing, reaction effluent afterheat utilization method in the ethylene production, processing step is: allow the steam flow be that the reaction effluent of 5t/h is flowed through one and continued to be connected with the heat exchanger 1 of boiler feedwater earlier, make in boiler feedwater intensification and the inflow boiler heating power oxygen-eliminating device, meanwhile, make reaction effluent cooling and obtain condensate liquid one time, then, a condensate liquid gravity flow enters one and continues to be connected with in another heat exchanger 2 of recirculated water, and obtains time condensation liquid.
The temperature of described reaction effluent is that 118 ℃, pressure are 0.12Mpa, and the temperature of a condensate liquid is 60 ℃, and the temperature of time condensation liquid is 25 ℃; The temperature of boiler feedwater water inlet is that 25 ℃, pressure are that 0.3～0.4Mpa, flow are 30t/h, and the temperature of boiler feedwater water outlet is that 95 ℃, pressure are 0.3～0.4Mpa; The temperature of recirculated water feedwater is 33 ℃, and the temperature of recirculated water backwater is 35 ℃.The described setting height(from bottom) that continues to be connected with the heat exchanger 1 of boiler feedwater is higher than the setting height(from bottom) of the heat exchanger 2 that continues to be connected with recirculated water.
Use this method, after the waste heat of reaction effluent was utilized, it is about 13% that the air demand of boiler improves, and the temperature of circulation has descended about 6 ℃, and ethene cost per ton descends 4～5%.
Above-described only is one embodiment of the present invention.Should be pointed out that for the person of ordinary skill of the art under the prerequisite that does not break away from the principle of the invention, can also make some modification and improvement, these also should be considered as belonging to protection scope of the present invention.
Claims (2)
1, reaction effluent afterheat utilization method in the ethylene production, processing step is: allow the reaction effluent heat exchanger that continues to be connected with boiler feedwater of flowing through earlier, make in boiler feedwater intensification and the inflow boiler heating power oxygen-eliminating device, meanwhile, make the reaction effluent cooling and obtain condensate liquid one time, then, a condensate liquid gravity flow enters one and continues to be connected with in another heat exchanger of recirculated water, and obtains time condensation liquid.
2, reaction effluent afterheat utilization method in the ethylene production according to claim 1, it is characterized in that: the temperature of reaction effluent is that 116～120 ℃, pressure are 0.1～0.13Mpa, the temperature of a condensate liquid is 50～80 ℃, and the temperature of time condensation liquid is 20～30 ℃; The temperature of boiler feedwater water inlet is that 20～30 ℃, pressure are 0.3～0.4Mpa, and the temperature of boiler feedwater water outlet is that 90～100 ℃, pressure are 0.3～0.4Mpa; The temperature of recirculated water feedwater is 30～35 ℃, and the temperature of recirculated water backwater is 33～37 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910034449A CN101644426A (en) | 2009-08-30 | 2009-08-30 | Afterheat utilization method of reaction effluent in ethane production |
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| Application Number | Priority Date | Filing Date | Title |
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| CN200910034449A CN101644426A (en) | 2009-08-30 | 2009-08-30 | Afterheat utilization method of reaction effluent in ethane production |
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| CN101644426A true CN101644426A (en) | 2010-02-10 |
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| CN200910034449A Pending CN101644426A (en) | 2009-08-30 | 2009-08-30 | Afterheat utilization method of reaction effluent in ethane production |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102330966A (en) * | 2011-08-17 | 2012-01-25 | 安阳方快锅炉有限公司 | Energy-saving heat-supplying device of condensation steam boiler |
| CN105085900A (en) * | 2014-05-13 | 2015-11-25 | 郑州大学 | Superheated steam recycling and waste heat utilizing apparatus |
-
2009
- 2009-08-30 CN CN200910034449A patent/CN101644426A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102330966A (en) * | 2011-08-17 | 2012-01-25 | 安阳方快锅炉有限公司 | Energy-saving heat-supplying device of condensation steam boiler |
| CN102330966B (en) * | 2011-08-17 | 2013-07-17 | 安阳方快锅炉有限公司 | Energy-saving heat-supplying device of condensation steam boiler |
| CN105085900A (en) * | 2014-05-13 | 2015-11-25 | 郑州大学 | Superheated steam recycling and waste heat utilizing apparatus |
| CN105085900B (en) * | 2014-05-13 | 2017-11-21 | 郑州大学 | A kind of superheated steam recovery and residual heat using device |
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Open date: 20100210 |