CN103121898A - Separating and recycling method of products containing ethylene - Google Patents
Separating and recycling method of products containing ethylene Download PDFInfo
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- CN103121898A CN103121898A CN2011103669057A CN201110366905A CN103121898A CN 103121898 A CN103121898 A CN 103121898A CN 2011103669057 A CN2011103669057 A CN 2011103669057A CN 201110366905 A CN201110366905 A CN 201110366905A CN 103121898 A CN103121898 A CN 103121898A
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Abstract
The invention relates to a separating and recycling method of products containing ethylene, and mainly solves the problems of high energy consumption and high operating cost in the prior art of producing ethylene with ethanol dehydration. According to the technical problem, a refrigerating fluid system is arranged, high-grade cooling capacity of a tower kettle of an ethylene dehygrpgenation tower is utilized to cool ethylene material flow of a discharging port of an ethylene compressor, and material flow quantity of heat of the discharging port of the ethylene compressor is utilized as a heat source of the ethylene dehygrpgenation tower reboiler, so that the problems are solved effectively, and the separating and recycling method can be adopted in industrial manufacture for producing the ethylene from ethanol.
Description
Technical field
The present invention relates to a kind of separation and recovery method that comprises the product logistics of ethene, particularly about the separation and recovery method of a kind of producing ethylene from dehydration of ethanol product logistics.
Background technology
In the method for industrial alcohol Dehydration ethene, do not relate to specially at present the patent of the comprehensive utilization aspect of energy, just mentioned the heat exchange aspect reactor input and output material the most basic in the total energy approach in Chinese patent CN101088975A.Yet in producing ethylene from dehydration of ethanol technique, the proportion that the energy consumption of rectifying tower, lightness-removing column etc. accounts in total energy consumption is quite large, demand for heat and higher-grade cold is also very large, so, only have the heat comprehensive utilization of considering whole device, just can reach the purpose that reduces running cost.
Summary of the invention
Technical problem to be solved by this invention is to have the problem that separating energy consumption is large, running cost is high in existing producing ethylene from dehydration of ethanol technique, and a kind of new separation and recovery method that contains ethylene product is provided.The method has simple to operate, and separating energy consumption is low, the advantage that running cost is low.
In order to solve the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of separation and recovery method that contains ethylene product, comprise the following steps: the product logistics 1 that a) comprises ethene enters the water wash column bottom, remove height and boil and discharge crude ethylene logistics 2 from tower top after component and part moisture, discharge process water at the bottom of tower; B) logistics 2 enters the bottom of water soda-wash tower, and after removing acidic substance, tower top obtains crude ethylene logistics 3, obtains process water at the bottom of tower; C) logistics 3 by ethylene compressor, ethene the first water cooler, ethene moisture eliminator and ethene the second water cooler, further removes moisture and obtains crude ethylene logistics 4 successively; D) logistics 4 enters ethylene rectification tower, obtains crude ethylene logistics 5 at tower top after removing heavy constituent; E) logistics 5 enters the ethene lightness-removing column, and tower top is discharged the light constituent that separates, and tower reactor obtains qualified ethylene product; Wherein, refrigerating fulid is used for the cooling of ethene the second water cooler and ethene the first water cooler as low-temperature receiver, refrigerating fulid after intensification is transported in ethene lightness-removing column reboiler and is used as thermal source, after reboiler, the refrigerating fulid recirculation that temperature descends is as the low-temperature receiver of ethene the second water cooler and ethene the first water cooler.
In technique scheme, the ethylene rectification tower tower reactor utilizes the process water of water wash system generation as thermal source; The top hole pressure of compressor is 1.00～4.00MPaG; The working pressure of ethylene rectification tower is 1.00～4.00MPaG; The working pressure of ethene lightness-removing column is 1.00～4.00MPaG.
In the present invention, by a cover refrigerating fulid system is set, utilize the higher-grade cold of ethene lightness-removing column tower reactor to come the ethylene streams of cooled ethylene compressor outlet, utilize the logistics heat of ethylene compressor outlet as the thermal source of ethene lightness-removing column reboiler, realize the comprehensive utilization of higher-grade energy, thereby greatly reduced system energy consumption.Utilize simultaneously the process water of water wash column generation as the thermal source of ethylene rectification tower reboiler, realized the comprehensive utilization of the process water heat that water wash system produces.By the comprehensive utilization of energy, the consumption of low-grade cold has reduced by 36.37%, and the consumption of higher-grade cold has reduced by 3.75%, and the consumption of tow taste heat has reduced by 37.34%, has obtained technique effect preferably.
Description of drawings
Fig. 1 is the technical process of producing ethylene from dehydration of ethanol of the present invention.
In Fig. 1,1 is reactor, and 2 is water wash column, 3 is the water soda-wash tower, and 4 is ethylene compressor, and 5 is ethene the first water cooler, 6 is the ethene moisture eliminator, 7 is ethene the second water cooler, and 8 is ethylene rectification tower, and 9 is the ethylene rectification tower reboiler, 10 is the ethene lightness-removing column, 11 is ethene lightness-removing column reboiler, and 12 is freezing liquid pump, and 13 is freezing liquid bath.
In Fig. 1, enter reactor 1 after being heated to certain temperature from out-of-bounds feed ethanol, dehydration generates ethene under the aluminium oxide catalyst effect.The cooling of reacted gas is laggard enters water wash column 2.Reactant gases enters from water wash column 2 bottoms, is ejected by water wash column 2 after removing large quantity of moisture and heavy constituent, then enters water soda-wash tower 3 bottoms.The process water that discharge the water wash column bottom is as the thermal source of ethylene rectification tower reboiler 9.Water soda-wash tower 3 tops gas out enters ethylene compressor 4 superchargings, then enters successively ethene the first water cooler 5, ethene moisture eliminator 6 and ethene the second water cooler 7 dehydrations and cooling.Then reaction product enters ethylene rectification tower 8 and ethene lightness-removing column 10, removes respectively heavy constituent and light constituent by low ternperature separation process, and the tower reactor from ethene lightness-removing column 10 obtains qualified ethylene product at last.Refrigerating fulid is used for the cooling of ethene the second water cooler 7 and ethene the first water cooler 5 as low-temperature receiver, the refrigerating fulid that freezing liquid bath 13 is collected after heating up, and be transported in ethene lightness-removing column reboiler 11 by freezing liquid pump 12 and be used as thermal source, after reboiler, the temperature of refrigerating fulid descends, can again as the low-temperature receiver of ethene the second water cooler 7 and ethene the first water cooler 5, circulate successively again.
The present invention is further elaborated below by embodiment.
Embodiment
[embodiment 1]
Reaction feed is the ethanol of 95.0 volume %, and temperature of reaction is 380 ℃, and reaction pressure is 0.05MPaG, and dehydration catalyst is aluminum oxide.The dehydration reaction crude product enters from the bottom of water wash column, and the process water that discharge the bottom is as the thermal source of ethylene rectification tower reboiler, through cooling and remove the height product that obtains after component and part moisture that boils and discharge from tower top, then enters the bottom of water soda-wash tower.Remove acidic substance in the water soda-wash tower after, reaction product enters in ethylene compressor, ethene the first water cooler, ethene moisture eliminator and ethene the second water cooler successively, removes moisture in the reaction product crude ethylene by these steps.Wherein, the top hole pressure of ethylene compressor is 2.00MPaG.Then reaction product enters ethylene rectification tower and ethene lightness-removing column, and working pressure is respectively 1.88MPaG and 2.10MPaG.Remove respectively heavy constituent and light constituent by low ternperature separation process in two towers, the tower reactor from the ethene lightness-removing column obtains qualified ethylene product at last.Wherein, the cooling of the heating of ethene lightness-removing column tower reactor and compressor outlet logistics realized by a cover refrigerating fulid system is set separately.The required low-grade cold of this flow process (water coolant) is 1.76MW, and higher-grade cold (propylene refrigerants of 40 ℃) is 1.62MW, and tow taste heat (low-pressure steam) is 1.89MW.
[embodiment 2]
Press condition and the step of embodiment 1, keep the operational condition of reactor constant, the top hole pressure that changes compressor is 4.00MPaG, and the working pressure that changes ethylene rectification tower and ethene lightness-removing column is respectively 3.88MPaG and 4.10MPaG.The required low-grade cold of this flow process is 5.28MW, and the higher-grade cold is 5.06MW, and tow taste heat is 6.42MW.
[embodiment 3]
Press condition and the step of embodiment 1, keep the operational condition of reactor constant, the top hole pressure that changes compressor is 1.50MPaG, and the working pressure that changes ethylene rectification tower and ethene lightness-removing column is respectively 1.38MPaG and 1.60MPaG.The required low-grade cold of this flow process is 2.58MW, and the higher-grade cold is 1.87MW, and tow taste heat is 2.82MW.
[embodiment 4]
Press condition and the step of embodiment 1, keep the operational condition of reactive system, ethylene rectification tower and ethene lightness-removing column constant, just the process water of water wash column bottom discharge is not used as the thermal source of ethylene rectification tower reboiler.The required low-grade cold of this flow process is 2.77MW, and the higher-grade cold is 1.56MW, and tow taste heat is 2.90MW.
[comparative example 1]
Press condition and the step of embodiment 1, keep the operational condition of reactive system, ethylene rectification tower and ethene lightness-removing column constant, the process water that discharge the water wash column bottom is not used as the thermal source of ethylene rectification tower reboiler, ethene lightness-removing column tower reactor does not arrange separately a cover refrigerating fulid system yet and heats, the required low-grade cold of this flow process is 2.77MW, the higher-grade cold is 1.68MW, and tow taste heat is 3.02MW.Namely in the situation that do not consider total energy approach, the consumption of low-grade cold increases by 57.15%, and the consumption of higher-grade cold increases by 3.90%, and the consumption of tow taste heat increases to 59.60%.
Claims (5)
1. separation and recovery method that contains ethylene product comprises the following steps:
A) the product logistics 1 that comprises ethene enters the water wash column bottom, removes height and boils and discharge crude ethylene logistics 2 from tower top after component and part moisture, discharges process water at the bottom of tower;
B) logistics 2 enters the bottom of water soda-wash tower, and after removing acidic substance, tower top obtains crude ethylene logistics 3, obtains process water at the bottom of tower;
C) logistics 3 by ethylene compressor, ethene the first water cooler, ethene moisture eliminator and ethene the second water cooler, further removes moisture and obtains crude ethylene logistics 4 successively;
D) logistics 4 enters ethylene rectification tower, obtains crude ethylene logistics 5 at tower top after removing heavy constituent;
E) logistics 5 enters the ethene lightness-removing column, and tower top is discharged the light constituent that separates, and tower reactor obtains qualified ethylene product;
Wherein, refrigerating fulid is used for the cooling of ethene the second water cooler and ethene the first water cooler as low-temperature receiver, refrigerating fulid after intensification is transported in ethene lightness-removing column reboiler and is used as thermal source, after reboiler, the refrigerating fulid recirculation that temperature descends is as the low-temperature receiver of ethene the second water cooler and ethene the first water cooler.
2. the separation and recovery method that contains ethylene product according to claim 1 is characterized in that the ethylene rectification tower tower reactor utilizes process water that water wash column produces as thermal source.
3. the method for producing ethylene from dehydration of ethanol according to claim 1, the top hole pressure that it is characterized in that compressor is 1.00～4.00MPaG.
4. the method for producing ethylene from dehydration of ethanol according to claim 1, the working pressure that it is characterized in that ethylene rectification tower is 1.00～4.00MPaG.
5. the method for producing ethylene from dehydration of ethanol according to claim 1, the working pressure that it is characterized in that the ethene lightness-removing column is 1.00～4.00MPaG.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201110366905.7A CN103121898B (en) | 2011-11-18 | 2011-11-18 | Separating and recycling method of products containing ethylene |
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| CN201110366905.7A CN103121898B (en) | 2011-11-18 | 2011-11-18 | Separating and recycling method of products containing ethylene |
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| CN103121898A true CN103121898A (en) | 2013-05-29 |
| CN103121898B CN103121898B (en) | 2015-04-08 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113527023A (en) * | 2020-04-15 | 2021-10-22 | 中国石油化工股份有限公司 | System and method for preparing propylene from isopropanol |
| EP4332076A2 (en) | 2022-08-30 | 2024-03-06 | Tianjin University | Thermal coupling method for preparing ethylene by ethanol dehydration and device thereof |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101134704A (en) * | 2007-10-16 | 2008-03-05 | 南京工业大学 | Process for producing ethylene by ethanol dehydration |
| CN101244970A (en) * | 2007-02-13 | 2008-08-20 | 广东中科天元新能源科技有限公司 | Apparatus and technique for producing ethylene with ethyl alcohol |
| CN101747136A (en) * | 2008-12-04 | 2010-06-23 | 焦作市河阳酒精实业有限公司 | Technique for producing ethylene through catalyzing and dehydrating ethanol |
-
2011
- 2011-11-18 CN CN201110366905.7A patent/CN103121898B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101244970A (en) * | 2007-02-13 | 2008-08-20 | 广东中科天元新能源科技有限公司 | Apparatus and technique for producing ethylene with ethyl alcohol |
| CN101134704A (en) * | 2007-10-16 | 2008-03-05 | 南京工业大学 | Process for producing ethylene by ethanol dehydration |
| CN101747136A (en) * | 2008-12-04 | 2010-06-23 | 焦作市河阳酒精实业有限公司 | Technique for producing ethylene through catalyzing and dehydrating ethanol |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113527023A (en) * | 2020-04-15 | 2021-10-22 | 中国石油化工股份有限公司 | System and method for preparing propylene from isopropanol |
| EP4332076A2 (en) | 2022-08-30 | 2024-03-06 | Tianjin University | Thermal coupling method for preparing ethylene by ethanol dehydration and device thereof |
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| CN103121898B (en) | 2015-04-08 |
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