CN112358375B - Two-tower double-heat-pump integrated 1-butene refining energy-saving process and device - Google Patents
Two-tower double-heat-pump integrated 1-butene refining energy-saving process and device Download PDFInfo
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Abstract
The invention relates to the technical field of 1-butene refining, in particular to a two-tower double-heat-pump integrated energy-saving process and a two-tower double-heat-pump integrated energy-saving device for 1-butene refining. According to the two-tower double-heat-pump integrated 1-butene refining energy-saving process, a mixture containing 1-butene, which is obtained by subjecting a mixture of ether and carbon of MTBE to selective hydrogenation, is subjected to heavy component removal through a heavy component removal tower, then is subjected to light component removal through a light component removal tower, and 1-butene is obtained from the bottom of the light component removal tower; the light component evaporated from the top of the heavy component removal tower is subjected to adiabatic compression and then is used as a heating medium of a reboiler of a heavy component removal tower 1 #; decompressing the 1-butene removed from the bottom of the light component removal tower to be used as a cold source medium of a condenser, cooling the light component evaporated from the top of the light component removal tower, gasifying the 1-butene, and then compressing the gasified 1-butene by adiabatic compression to return to the bottom of the light component removal tower. The invention utilizes the technical means of the heat pump to establish the heat pump rectification system of the heavy component removal tower and the light component removal tower and the energy integration of waste heat recycling, and increases the economic benefit under the condition of meeting the requirements of product indexes and yield.
Description
Technical Field
The invention relates to the technical field of 1-butene refining, in particular to a two-tower double-heat-pump integrated energy-saving process and a two-tower double-heat-pump integrated energy-saving device for 1-butene refining.
Background
1-butene (C) 4 H 8 ) Is an important chemical raw material, and is mainly used as a comonomer for producing Linear Low Density Polyethylene (LLDPE) and poly-1-butylene plastics. With the continuous development of chemical industry in China, particularly the continuous increase of byproduct mixed C4 resources in petrochemical industry and coal chemical industry, 1-butene produced by the C4 separation method is increased year by year, thereby driving the development of 1-butene industry.
At present, the production of 1-butene in China mainly adopts a mixed C4 separation method, and mixed C4 mainly comes from a steam cracking device, a catalytic cracking (FCC) device and a coal-to-olefin (MTO) device in the petrochemical industry. The by-product mixed C4 in petrochemical and coal chemical industries contains a large amount of 1-butene, butane, butadiene, 2-butene, isobutene and other components although the components are different. The process comprises the steps of extracting butadiene by using an extractive distillation device, and removing isobutene in raffinate by an MTBE (methyl tert-butyl ether) method. And removing trace butadiene from the etherified mixed C4 by a hydrogenation method, and finally performing an ultra-precise rectification separation method, wherein the ultra-precise rectification separation method comprises a light component removal tower and a heavy component removal tower, the light component removal tower is used for removing carbon three, isobutane and azeotrope with water with low boiling point in carbon four, the light component removal tower is used for removing high boiling point n-butane and 2-butene from a tower bottom product by the heavy component removal tower, and the tower top is used for obtaining 1-butene with the mass fraction of more than 99.3%. Although the process has simple flow, the required number of tower plates is large, the reflux ratio is large, and the energy consumption is high. How to reduce the energy consumption of the device and improve the economic benefit of the device is a problem to be solved as soon as possible.
Patent CN2014101190893 discloses an energy-saving process flow for 1-butene separation and purification, wherein after etherification carbon-four mixture from MTBE is subjected to selective hydrogenation reaction, lighter isobutane components are removed through a deisobutanizer and a rectifying tower, and simultaneously H 2 、H 2 O, methanol and hydrocarbons form a low-boiling-point azeotrope which is removed from the top of the tower, then heavier components of n-butane, trans-2-butene and cis-2-butene are removed through a 1-butene rectifying tower, and high-purity 1-butene can be obtained from the top of the tower.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide a 1-butene refining energy-saving process and a device with two towers and double heat pumps integrated, a heat pump rectification system of a heavy component removal tower and a light component removal tower and energy integration of waste heat recycling are established by using a technical means of a heat pump, the economic benefit of the device is increased under the condition of meeting the requirements of 1-butene product indexes and yield, and the device is simple and convenient to operate.
According to the two-tower double-heat-pump integrated 1-butene refining energy-saving process, after ether and carbon four mixture of MTBE is subjected to selective hydrogenation reaction, a 1-butene-containing mixture with the main components of hydrogen, water, methanol, carbon three, 1-butene, isobutane, n-butane, trans-2-butene and cis-2-butene is obtained, heavy components containing n-butane, trans-2-butene and cis-2-butene are removed through a heavy component removing tower, light components containing isobutane and carbon three are removed through a light component removing tower, and 1-butene is obtained from the bottom of the light component removing tower;
wherein, the light component evaporated from the top of the heavy component removal tower is used as a heating medium of a reboiler of a heavy component removal tower No. 1 after adiabatic compression;
and (3) decompressing the 1-butene desorbed from the bottom of the light component removal tower to serve as a cold source medium of a condenser, cooling the light component containing carbon III and isobutane evaporated from the top of the light component removal tower, gasifying the 1-butene, and then compressing the gasified 1-butene through adiabatic compression to return to the bottom of the light component removal tower.
The heavy component removing tower and the light component removing tower are both set as packed towers, and high-efficiency packing with small pressure drop and high-efficiency mass transfer capacity is selected and is respectively a tower.
Specifically, the two-tower double-heat-pump integrated 1-butene refining energy-saving process comprises the following steps:
(1) after the ether post-carbon-four mixture of MTBE is subjected to selective hydrogenation reaction, a 1-butene-containing mixture with the main components of hydrogen, water, methanol, carbon three, 1-butene, isobutane, n-butane, trans-2-butene and cis-2-butene is obtained, the 1-butene-containing mixture is subjected to heat exchange through a # 1 heat exchanger and then enters a de-weighting tower for rectification, heavy components containing n-butane, trans-2-butene and cis-2-butene are removed from the bottom of the de-weighting tower, and the heavy components are cooled through the # 2 heat exchanger and then are sent out of the device;
(2) the heavy component removal tower adopts a tower top steam recompression type heat pump technology, light components containing 1-butene and isobutane are evaporated from the tower top of the heavy component removal tower, the pressure and the temperature are improved after the light components are compressed by a 1# compressor, the light components return to a 1# reboiler of the heavy component removal tower to be used as a heating medium, the temperature is reduced after the light components are subjected to heat exchange by the 1# reboiler to be a full liquid phase, the full liquid phase enters an air cooler to be further cooled to a supercooled state, the pressure is reduced by a 1# throttle valve, the full liquid phase enters a 1# reflux tank, a part of the liquid phase cooled in the 1# reflux tank is used as reflux to the tower top of the heavy component removal tower, the heat pump rectification process is completed, and the rest part of the liquid phase enters a light component removal tower to be rectified;
(3) the light component removing tower adopts a tower bottom liquid flash evaporation recompression type heat pump technology, 1-butene is removed from the bottom of the light component removing tower, one part of the 1-butene is sent out of the device after being cooled, the rest part of the 1-butene is decompressed through a 2# throttle valve and enters a condenser for gasification, so that cold energy is provided for the condenser, the pressure and the temperature of the gasified material are improved after being compressed by a 2# compressor, and then the gasified material returns to the tower bottom of the light component removing tower to finish the heat pump rectification process; and (3) distilling out light components containing the carbon three and the isobutane from the top of the light component removal tower, cooling the light components by a condenser and a 4# heat exchanger, then feeding the light components into a 2# reflux tank, feeding noncondensable gas containing a small amount of the carbon three and the hydrogen out of the device from the top of the 2# reflux tank, feeding a part of liquid materials into the top of the light component removal tower to serve as reflux, and feeding the rest of the liquid materials out of the device as light carbon four rich in the isobutane.
The pressure at the top of the de-heavy tower is 0.45-1 MPaG, the temperature at the top of the de-heavy tower is 45-65 ℃, the pressure at the bottom of the de-heavy tower is 0.55-1.1 MPaG, the temperature at the bottom of the de-heavy tower is 65-85 ℃, and the reflux ratio at the top of the de-heavy tower is 8-20.
The top pressure of the light component removal tower is 0.5-1.1 MPaG, the temperature of the top of the tower is 45-65 ℃, the pressure of the bottom of the tower is 0.6-1.2 MPaG, the temperature of the bottom of the tower is 60-80 ℃, and the reflux ratio of the top of the tower is 100-300.
The heavy component removal tower also provides heat through an auxiliary reboiler, the auxiliary reboiler is heated by steam, and steam condensate is introduced into a No. 1 heat exchanger to serve as a heating medium; when the light component removal tower is started, the heat pump rectification system cannot be used, and heat is provided through the 2# reboiler.
And (3) distilling out light components containing 1-butene and isobutane from the top of the heavy component removal tower, compressing by a No. 1 compressor, and then, controlling the temperature to be 75-100 ℃ and the pressure to be 1.1-1.8 MpaG.
And when the 1-butene returns to the tower kettle of the light component removal tower, the temperature is 60-85 ℃, and the pressure is 0.75-1.25 MPaG.
The invention relates to a 1-butene refining energy-saving device with two towers and double heat pumps integrated, which comprises a heat exchange unit, a rectification unit, a compression unit and a fluid conveying unit; the heat exchange unit comprises a reboiler, a heat exchanger, a condenser and an air cooler; the rectification unit comprises a heavy component removing tower and a light component removing tower.
Specifically, the energy-saving device for refining 1-butene with two towers and double heat pumps is integrated and comprises a feeding pipe, a heavy component removal tower and a light component removal tower; the feeding pipe passes through the No. 1 heat exchanger and is connected with a feeding port of the de-weighting tower; the tower bottom of the heavy component removal tower is connected with an auxiliary reboiler and a # 1 reboiler, wherein the auxiliary reboiler is connected with a # 1 heat exchanger; a discharge port at the bottom of the tower of the de-heavy tower is connected with a heavy component recovery pipeline; a discharge port at the top of the heavy component removal tower is sequentially connected with a 1# compressor, a 1# reboiler, an air cooler, a 1# throttle valve and a 1# reflux tank, and the 1# reflux tank is respectively connected with a reflux port at the top of the heavy component removal tower and a feed inlet of the light component removal tower through a 1# reflux pump; the tower bottom of the light component removal tower is connected with a 2# reboiler; the tower bottom discharge of the light component removal tower is divided into two paths, one path is connected with a 1-butene recovery pipeline, and the other path is connected with a tower kettle feed inlet of the light component removal tower through a 2# throttle valve, a condenser and a 2# compressor in sequence; the discharge port at the top of the light component removing tower is sequentially connected with a condenser, a 4# heat exchanger and a 2# reflux tank, and the 2# reflux tank is respectively connected with the reflux port at the top of the light component removing tower and a light carbon four-recovery pipeline through a 2# reflux pump.
The 2# backflow tank is connected with a noncondensable gas pipeline.
And a discharge port at the bottom of the tower of the de-heavy tower is connected with a heavy component recovery pipeline through a No. 1 tower bottom pump and a No. 2 heat exchanger.
The bottom discharge of the light component removal tower is divided into two paths, wherein one path is connected with a 1-butylene recovery pipeline through a No. 2 tower bottom pump and a No. 3 heat exchanger.
The working process of the 1-butene refining energy-saving device with two towers and two heat pumps is as follows:
the etherified C-C mixture from MTBE is subjected to selective hydrogenation reaction, and the main components of the etherified C-C mixture are hydrogen, water, methanol, C-C, 1-butene, isobutane, n-butane, trans-2-butene and cis-2-butene. And (2) after the heat exchange of the mixture is carried out by a No. 1 heat exchanger, the mixture enters a de-weighting tower for rectification, wherein heavy components containing n-butane, trans-2-butene and cis-2-butene are removed from the bottom of the de-weighting tower, are pumped out by a No. 1 tower bottom pump, enter a No. 2 heat exchanger for heat exchange and are cooled, and then are introduced into a heavy component recovery pipeline.
The heavy component removal tower adopts a tower top steam recompression type heat pump technology, light components containing 1-butene and isobutane are evaporated from the tower top of the heavy component removal tower, the pressure and the temperature of gas at the tower top are improved after the gas enters a compressor 1# and is compressed, a reboiler 1# which returns to the heavy component removal tower is used as a heating medium to provide heat for the heavy component removal tower, the temperature of gas materials at the tower top is reduced after heat exchange, the gas materials at the tower top become a full liquid phase, the gas materials enter an air cooler and are further cooled to a supercooled state, and the gas materials are decompressed through a throttle valve 1# and enter a reflux tank 1# after the pressure and the temperature of the gas materials at the tower top are reduced; an auxiliary reboiler of the de-heavy tower is heated by steam to provide insufficient heat for the reboiler No. 1, steam condensate is sent to the heat exchanger No. 1 to serve as a heating source, when the vehicle is started, the heat pump rectification system cannot be put into use, and the auxiliary reboiler is required to provide all heat; after the pressure of the liquid phase cooled in the 1# reflux tank is increased by a 1# reflux pump, one part of the liquid phase returns to the top of the heavy component removal tower as reflux to finish the heat pump rectification process, and the other part of the liquid phase enters a light component removal tower to be rectified.
The lightness-removing tower adopts a tower bottom flash evaporation recompression type heat pump technology, the material at the bottom of the lightness-removing tower is 1-butylene, one part of the material is pumped out by a No. 2 tower bottom pump, enters a No. 3 heat exchanger for heat exchange and temperature reduction and then is introduced into a 1-butylene recovery pipeline, the other part of the material is decompressed by a No. 2 throttle valve and enters a condenser for gasification, cold energy is provided for the condenser, the pressure and the temperature of the gasified material are improved after the gasified material enters a No. 2 compressor for compression, and then the gasified material returns to the tower bottom of the lightness-removing tower to finish the heat pump rectification process; when the vehicle is started, the heat pump rectification system can not be used, and a 2# reboiler is started to provide all heat for the light component removal tower; and (3) distilling out light components such as carbon three and isobutane from the top of the light component removal tower, cooling the light components by a condenser and a 4# heat exchanger, feeding the light components into a 2# reflux tank, feeding noncondensable gas containing a small amount of light components such as carbon three and hydrogen out of the device from the top of the 2# reflux tank, pumping out a liquid material by a 2# reflux pump, feeding a part of the liquid material into the top of the light component removal tower as reflux, and feeding a part of the liquid material out of the device as light carbon four rich in isobutane.
Compared with the prior art, the invention has the following beneficial effects:
(1) the whole process and the device adopt two packed tower processes with high-efficiency separation, and establish a heat pump rectification system of a heavy component removal tower and a light component removal tower and energy integration of waste heat recycling by using the technical means of a heat pump, wherein the heavy component removal tower adopts a tower top steam recompression type heat pump, and the light component removal tower adopts a tower kettle flash evaporation recompression type heat pump, so that high-efficiency energy-saving separation of high-purity 1-butene is realized, the consumption of steam and circulating water is greatly reduced, the working pressure of the tower is low, the operation is simple, the occupied area is small, the economic benefit of the device is improved, and the device is environment-friendly;
(2) the invention changes the traditional mode of removing light and heavy firstly and then removing heavy, firstly removes heavy components such as normal butane, trans-2-butene and cis-2-butene and the like through a heavy removal tower, then removes light components such as isobutane and carbon, and the like, and can obtain high-purity 1-butene from the tower bottom.
Drawings
FIG. 1 is a schematic diagram of the structure of a 1-butene refining energy-saving device with two-tower double-heat-pump integration;
in the figure: 1. a feeding pipe; 2. 1# heat exchanger; 3. a de-weighting tower; 4. 1# compressor; 5. a light component removal tower; 6. a condenser; 7. a No. 2 throttle valve; 8. 2# compressor; 9. 4# heat exchanger; 10. a No. 2 reflux tank; 11. a noncondensable gas pipeline; 12. an auxiliary reboiler; 13. 1# bottom pump; 14. a # 1 reboiler; 15. 2# heat exchanger; 16. a heavy component recovery line; 17. an air cooler; 18. a No. 1 throttle valve; 19. 1# reflux tank; 20. 1# reflux pump; 21. a # 2 reboiler; 22. 2# bottom column pump; 23. a No. 3 heat exchanger; 24. a 1-butene recovery line; 25. 2# reflux pump; 26. and a light carbon four recovery pipeline.
Detailed Description
The present invention is further illustrated by the following examples, but the scope of the invention is not limited thereto.
Example 1
As shown in figure 1, the 1-butene refining energy-saving device with two towers and double heat pumps is integrated and comprises a feeding pipe 1, a heavy component removal tower 3 and a light component removal tower 5; a feeding pipe 1 passes through a No. 1 heat exchanger 2 and then is connected with a feeding hole of a de-weighting tower 3; the tower bottom of the heavy component removal tower 3 is connected with an auxiliary reboiler 12 and a # 1 reboiler 14, wherein the auxiliary reboiler 12 is connected with the # 1 heat exchanger 2; a discharge hole at the bottom of the heavy component removal tower 3 is connected with a heavy component recovery pipeline 16; a discharge port at the top of the heavy component removal tower 3 is sequentially connected with a 1# compressor 4, a 1# reboiler 14, an air cooler 17, a 1# throttle valve 18 and a 1# reflux tank 19, and the 1# reflux tank 19 is respectively connected with a reflux port at the top of the heavy component removal tower 3 and a feed port of the light component removal tower 5 through a 1# reflux pump 20; the tower bottom of the light component removal tower 5 is connected with a 2# reboiler 21; the tower bottom discharge of the light component removal tower 5 is divided into two paths, one path is connected with a 1-butylene recovery pipeline 24, and the other path is connected with a tower kettle feed inlet of the light component removal tower 5 through a No. 2 throttle valve 7, a condenser 6 and a No. 2 compressor 8 in sequence; the discharge port at the top of the light component removal tower 5 is sequentially connected with a condenser 6, a 4# heat exchanger 9 and a 2# reflux tank 10, and the 2# reflux tank 10 is respectively connected with the reflux port at the top of the light component removal tower 5 and a light carbon four-recovery pipeline 26 through a 2# reflux pump 25.
The 2# return tank 10 is connected with a non-condensable gas pipeline 11.
The discharge hole at the bottom of the heavy component removal tower 3 is connected with a heavy component recovery pipeline 16 through a No. 1 tower bottom pump 13 and a No. 2 heat exchanger 15.
The bottom discharge of the light component removal tower 5 is divided into two paths, wherein one path is connected with a 1-butene recovery pipeline 24 through a No. 2 tower bottom pump 22 and a No. 3 heat exchanger 23.
The working process of the energy-saving device for refining 1-butene with two towers and two heat pumps is as follows:
the etherified C-C mixture from MTBE is subjected to selective hydrogenation reaction, and the main components of the etherified C-C mixture are hydrogen, water, methanol, C-C, 1-butene, isobutane, n-butane, trans-2-butene and cis-2-butene. The mixture is subjected to heat exchange by a # 1 heat exchanger 2, and then enters a de-heavy tower 3 for rectification, wherein heavy components containing normal butane, trans-2-butene and cis-2-butene are removed from the bottom of the de-heavy tower 3, pumped out by a # 1 tower bottom pump 13, enter a # 2 heat exchanger 15 for heat exchange and are cooled, and then enter a heavy component recovery pipeline 16.
The heavy component removal tower 3 adopts a tower top steam recompression type heat pump technology, light components containing 1-butene and isobutane are evaporated from the tower top of the heavy component removal tower 3, the pressure and the temperature of gas at the tower top are improved after the gas enters a compressor 4 No. 1 and is compressed, a reboiler No. 1 14 returning to the heavy component removal tower 3 is used as a heating medium to provide heat for the heavy component removal tower 3, the temperature of the gas material at the tower top is reduced after heat exchange to form a full liquid phase, the full liquid phase enters an air cooler 17 and is further cooled to a supercooled state, the pressure is reduced through a throttle valve 18 No. 1, and the full liquid phase enters a reflux tank 19 No. 1; an auxiliary reboiler 12 of the de-heavy tower 3 is heated by steam to provide insufficient heat for a 1# reboiler 14, steam condensate is sent to a 1# heat exchanger 2 to serve as a heating source, when the vehicle is started, a heat pump rectification system cannot be used, and the auxiliary reboiler 12 is required to provide all heat; after the pressure of the liquid phase cooled in the 1# reflux tank 19 is increased by the 1# reflux pump 20, one part of the liquid phase returns to the top of the heavy component removal tower 3 as reflux to finish the heat pump rectification process, and the other part of the liquid phase enters the light component removal tower 5 for rectification.
The lightness-removing tower 5 adopts a tower bottom flash evaporation and recompression type heat pump technology, the material at the bottom of the lightness-removing tower 5 is 1-butene, one part of the material is pumped out by a No. 2 tower bottom pump 22, enters a No. 3 heat exchanger 23 for heat exchange and temperature reduction, then is introduced into a 1-butene recovery pipeline 24, the other part of the material is decompressed by a No. 2 throttle valve 7, enters a condenser 6 for gasification, cold energy is provided for the condenser 6, the pressure and the temperature of the gasified material are improved after entering a No. 2 compressor 8 for compression, and then the gasified material returns to the tower bottom of the lightness-removing tower 5 to finish the heat pump rectification process; when the vehicle is started, the heat pump rectification system can not be used, and the 2# reboiler 21 is started to provide all heat for the light component removal tower; and (3) evaporating light components such as carbon, three, isobutane and the like from the top of the light component removal tower 5, cooling the light components by a condenser 6 and a 4# heat exchanger 9, then feeding the light components into a 2# reflux tank 10, sending non-condensable gas containing a small amount of light components such as carbon, three and hydrogen out of the device from the top of the 2# reflux tank 10, pumping the liquid material out by a 2# reflux pump 25, feeding a part of the liquid material into the top of the light component removal tower 5 as reflux, and feeding a part of the liquid material out of the device as light carbon rich in isobutane.
Example 2
The energy-saving device for refining 1-butene, which is integrated by two towers and two heat pumps and is used for refining 1-butene in the embodiment 1, comprises the following specific process flows:
the etherified C-C mixture from MTBE was subjected to a selective hydrogenation reaction to obtain a 1-butene-containing mixture having the main components hydrogen, water, methanol, C-C, 1-butene, isobutane, n-butane, trans-2-butene and cis-2-butene, the 1-butene-containing mixture having a temperature of 40 ℃ and a flow rate of 5507.41kg/h and having the composition shown in Table 1.
TABLE 1 composition of the 1-butene-containing mixtures
| Composition of | Hydrogen gas | Water (I) | Carbon III | Isobutane | N-butane | 1-butene | Isobutene |
| kg/h | 0.3333 | 4.626 | 18.906 | 172.044 | 1138.344 | 3397.1 | 2.968 |
| Composition of | Cis-2-butene | Trans-2-butene | Butadiene | Vinyl acetylene | Methanol | MTBE | Dimethyl ether |
| kg/h | 443.866 | 327.587 | 0.055 | 0.048 | 0.249 | 0.00095 | 1.283 |
And (2) after heat exchange of the mixture by a No. 1 heat exchanger, raising the temperature to 56 ℃, introducing the mixture into a de-heavy column for rectification, wherein the pressure at the top of the de-heavy column is 0.6MPaG, the temperature at the top of the de-heavy column is 55.5 ℃, the pressure at the bottom of the de-heavy column is 0.71MPaG, the temperature at the bottom of the de-heavy column is 70.9 ℃, and the reflux ratio at the top of the de-heavy column is 12.6. Wherein heavy components (the flow rate is 1925.72kg/h, the temperature is 70.9 ℃) containing n-butane, trans-2-butene and cis-2-butene are removed from the bottom of the de-weighting tower, are pumped out by a No. 1 tower bottom pump, enter a No. 2 heat exchanger for heat exchange and are cooled to 40 ℃, and then are sent out of the device.
The heavy component removal tower adopts a tower top steam recompression type heat pump technology, light components containing 1-butene and isobutane are evaporated from the tower top of the heavy component removal tower (the flow is 48828kg/h and the temperature is 55.5 ℃), the light components enter a No. 1 compressor to be compressed, the pressure is increased to 1.3MPaG, the temperature is increased to 86.9 ℃, a No. 1 reboiler returning to the heavy component removal tower is used as a heating medium to provide heat for the heavy component removal tower, the temperature is reduced to 80.3 ℃ after heat exchange of the No. 1 reboiler to form a full liquid phase, the full liquid phase enters an air cooler to be further cooled to a supercooled state, the pressure is reduced through a No. 1 throttle valve, the temperature is reduced to 42.5 ℃, the pressure is reduced to 0.57MPaG, and the full liquid phase enters a No. 1 reflux tank; an auxiliary reboiler of the de-heavy tower is heated by steam to provide insufficient heat for the reboiler No. 1, steam condensate is sent to the heat exchanger No. 1 to serve as a heating source, when the vehicle is started, the heat pump rectification system cannot be put into use, and the auxiliary reboiler is required to provide all heat; after the pressure of the liquid phase cooled in the 1# reflux tank is increased by a 1# reflux pump, one part (the flow rate of 45246.4kg/h) returns to the top of the heavy component removal tower as reflux to finish the heat pump rectification process, and the other part (the flow rate of 3579.75kg/h) enters a light component removal tower for rectification.
The lightness-removing tower adopts a tower bottom flash evaporation recompression type heat pump technology, the top pressure of the lightness-removing tower is 0.65MPaG, the temperature of the top of the lightness-removing tower is 48.9 ℃, the pressure of the bottom of the lightness-removing tower is 0.76MPaG, the temperature of the bottom of the light-removing tower is 64.8 ℃, and the reflux ratio of the top of the lightness-removing tower is 170.5. The material at the bottom of the light component removal tower is 1-butene, one part (the flow rate is 3369.95kg/h) is pumped out by a No. 2 tower bottom pump, enters a No. 3 heat exchanger for heat exchange and is cooled to 40 ℃, and is sent out of the device, the other part (the flow rate is 41474.7kg/h) is decompressed to 0.3MPaG through a No. 2 throttle valve and then enters a condenser for gasification, so that cold energy is provided for the condenser, the temperature is reduced to 34.7 ℃, the pressure of the gasified material is increased to 0.8MPaG after the material enters a No. 2 compressor for compression, the temperature is increased to 68.5 ℃, and the gasified material returns to the bottom of the light component removal tower to finish the heat pump rectification process; when the vehicle is started, the heat pump rectification system cannot be put into use, and a 2# reboiler is started to provide all heat for the light component removal tower; distilling out light components containing carbon, three and isobutane from the top of the light component removal tower (the flow is 35981.2kg/h, the temperature is 48.9 ℃), cooling the components by a condenser and a 4# heat exchanger, reducing the temperature to 45 ℃, feeding the components into a 2# reflux tank, sending noncondensable gas containing a small amount of light components such as carbon, three and hydrogen out of the device from the top of the 2# reflux tank, pumping out a liquid material by a 2# reflux pump, feeding a part (the flow is 35771.4kg/h) into the top of the light component removal tower as reflux, and feeding a part (the flow is 101.8kg/h) as light carbon rich in isobutane out of the device.
The composition of the main streams in the above process scheme is shown in table 2.
TABLE 2 composition of the major streams in the Process
Comparative example 1
In this comparative example, a mixture containing 1-butene was purified by the conventional rectification method of removing light and heavy components, wherein the mixture containing 1-butene was the same as in example 2, the temperature was 40 ℃ and the flow rate was 5507.41kg/h, and the composition was as shown in Table 1.
The rectification method comprises the following steps: firstly, removing low-boiling-point carbon three, isobutane and azeotrope with water by using a light component removal tower, wherein the top pressure of the light component removal tower is 0.65MPaG, the temperature at the top of the tower is 46.5 ℃, the pressure at the bottom of the tower is 0.76MPaG, the temperature at the bottom of the tower is 67.7 ℃, and the reflux ratio at the top of the tower is 195; then removing high-boiling-point n-butane and 2-butene by a de-heavy tower, wherein the pressure at the top of the de-heavy tower is 0.5MPaG, the temperature at the top of the de-heavy tower is 50 ℃, the pressure at the bottom of the de-heavy tower is 0.61MPaG, the temperature at the bottom of the de-heavy tower is 65.3 ℃, and the reflux ratio at the top of the de-heavy tower is 12.9; finally, 1-butene with the purity of 99.8 percent is obtained from the top of the de-heavy tower; all the equipment needing to be heated is heated by adopting steam, and all the equipment needing to be cooled is cooled by adopting circulating condensed water.
Comparative example 2
In the comparative example, the 1-butene-containing mixture was purified by a rectification method of removing heavy components first and then removing light components without heat pump heat integration, wherein the 1-butene-containing mixture was the same as in example 2, the temperature was 40 ℃, the flow rate was 5507.41kg/h, and the composition was as shown in Table 1.
The rectification method comprises the following steps: firstly, removing heavy components containing n-butane, trans-2-butene and cis-2-butene by using a de-heavy tower, wherein the pressure at the top of the de-heavy tower is 0.6MPaG, the temperature at the top of the de-heavy tower is 55.5 ℃, the pressure at the bottom of the de-heavy tower is 0.71MPaG, the temperature at the bottom of the de-heavy tower is 70.9 ℃, and the reflux ratio at the top of the de-heavy tower is 12.6; removing light components containing carbon, three and isobutane by using a light component removal tower, wherein the top pressure of the light component removal tower is 0.65MPaG, the temperature of the top of the light component removal tower is 48.9 ℃, the pressure of the bottom of the light component removal tower is 0.76MPaG, the temperature of the bottom of the light component removal tower is 64.8 ℃, and the reflux ratio of the top of the light component removal tower is 170; finally, 1-butene with the purity of 99.8 percent is obtained from the bottom of the light component removal tower; all the equipment needing heating is heated by adopting steam, and all the equipment needing cooling is cooled by adopting circulating condensed water.
Comparative example 3
The 1-butene-containing mixture was purified and refined by the rectification method of patent CN2014101190893, wherein the temperature of the 1-butene-containing mixture was 40 ℃, the flow rate was 5507.41kg/h, and the composition is shown in table 1. The process parameters were calculated by simulations exactly according to the data disclosed in example 1 thereof.
The top pressure of the lightness-removing column is 1.2MPaG, the temperature at the top of the column is 70.6 ℃, the pressure at the bottom of the column is 1.31MPaG, the temperature at the bottom of the column is 90.6 ℃, and the reflux ratio at the top of the column is 414.9.
The pressure at the top of the de-heavy tower is 1.7MPaG, the temperature at the top of the de-heavy tower is 99.9 ℃, the pressure at the bottom of the de-heavy tower is 1.81MPaG, the temperature at the bottom of the de-heavy tower is 112.3 ℃, and the reflux ratio at the top of the de-heavy tower is 48.3.
The results of comparing example 2 and comparative examples 1 to 3, in which the energy consumption in the distillation processes of example 2 and comparative examples 1 to 3 was converted into standard oil by calculating the recovery rate of 1-butene to be 99% and the purity to be 99.8%, simulating by chemical engineering simulation software Aspen Plus, and performing energy consumption conversion by GB/T50441-.
TABLE 3 comparison of energy consumption consumed by the rectification Processes of example 2 and comparative examples 1-3
As can be seen from Table 3, the energy-saving process for refining 1-butene with two-tower double-heat-pump integration of the invention has the obvious energy-saving characteristic when the 1-butene-containing mixture with the main components of hydrogen, water, methanol, carbon three, 1-butene, isobutane, n-butane, trans-2-butene and cis-2-butene is obtained after the carbon four mixture is subjected to selective hydrogenation reaction after the ether from MTBE is treated. Compared with the conventional rectification process of firstly removing light and then removing heavy, the energy consumption is reduced by about 69 percent; compared with the rectification process without heat pump heat integration, which is characterized in that the rectification process of removing heavy components first and removing light components later is carried out, the energy consumption is reduced by about 67 percent; compared with the rectification method in the prior patent CN2014101190893, the energy consumption is reduced by about 76%.
Claims (7)
1. A two-tower double-heat-pump integrated 1-butene refining energy-saving process is characterized by comprising the following steps: the method comprises the following steps:
(1) after the ether post-carbon-four mixture of MTBE is subjected to selective hydrogenation reaction, a 1-butene-containing mixture with the main components of hydrogen, water, methanol, carbon three, 1-butene, isobutane, n-butane, trans-2-butene and cis-2-butene is obtained, the 1-butene-containing mixture is subjected to heat exchange through a # 1 heat exchanger and then enters a de-weighting tower for rectification, heavy components containing n-butane, trans-2-butene and cis-2-butene are removed from the bottom of the de-weighting tower, and the heavy components are cooled through the # 2 heat exchanger and then are sent out of the device;
(2) the heavy component removal tower adopts a tower top steam recompression type heat pump technology, light components containing 1-butene and isobutane are evaporated from the tower top of the heavy component removal tower, the pressure and the temperature are improved after the light components are compressed by a 1# compressor, the light components return to a 1# reboiler of the heavy component removal tower to be used as a heating medium, the temperature is reduced after the light components are subjected to heat exchange by the 1# reboiler to be a full liquid phase, the full liquid phase enters an air cooler to be further cooled to a supercooled state, the pressure is reduced by a 1# throttle valve, the full liquid phase enters a 1# reflux tank, a part of the liquid phase cooled in the 1# reflux tank is used as reflux to the tower top of the heavy component removal tower, the heat pump rectification process is completed, and the rest part of the liquid phase enters a light component removal tower to be rectified;
(3) the light component removing tower adopts a tower bottom liquid flash evaporation recompression type heat pump technology, 1-butene is removed from the bottom of the light component removing tower, one part of the 1-butene is sent out of the device after being cooled, the rest part of the 1-butene is decompressed through a 2# throttle valve and enters a condenser for gasification, so that cold energy is provided for the condenser, the pressure and the temperature of the gasified material are improved after being compressed by a 2# compressor, and then the gasified material returns to the tower bottom of the light component removing tower to finish the heat pump rectification process; and distilling out light components containing the carbon three and the isobutane from the top of the light component removal tower, cooling the light components by a condenser and a 4# heat exchanger, feeding the light components into a 2# reflux tank, feeding noncondensable gas containing a small amount of the carbon three and the hydrogen out of the device from the top of the 2# reflux tank, feeding a part of liquid materials into the top of the light component removal tower as reflux, and feeding the rest of the liquid materials out of the device as light carbon four rich in the isobutane.
2. The two-tower double-heat-pump integrated energy-saving process for refining 1-butene according to claim 1, characterized in that: the pressure at the top of the de-heavy tower is 0.45-1 MPaG, the temperature at the top of the de-heavy tower is 45-65 ℃, the pressure at the bottom of the de-heavy tower is 0.55-1.1 MPaG, the temperature at the bottom of the de-heavy tower is 65-85 ℃, and the reflux ratio at the top of the de-heavy tower is 8-20.
3. The two-tower double-heat-pump integrated energy-saving process for refining 1-butene according to claim 1, characterized in that: the top pressure of the light component removal tower is 0.5-1.1 MPaG, the temperature of the top of the tower is 45-65 ℃, the pressure of the bottom of the tower is 0.6-1.2 MPaG, the temperature of the bottom of the tower is 60-80 ℃, and the reflux ratio of the top of the tower is 100-300.
4. The two-tower double-heat-pump integrated energy-saving process for refining 1-butene according to claim 1, characterized in that: the heavy component removal tower also provides heat through an auxiliary reboiler, the auxiliary reboiler is heated by steam, and steam condensate is introduced into a heat exchanger 1 to serve as a heating medium.
5. The two-tower double-heat-pump integrated 1-butene refining energy-saving process according to claim 1, characterized in that: when the light component removal tower is started, the heat pump rectification system cannot be used, and heat is provided through the 2# reboiler.
6. The two-tower double-heat-pump integrated energy-saving process for refining 1-butene according to claim 1, characterized in that: and distilling out light components containing 1-butene and isobutane from the top of the heavy component removal tower, and compressing the light components by using a 1# compressor at the temperature of 75-100 ℃ and the pressure of 1.1-1.8 MpaG.
7. The two-tower double-heat-pump integrated energy-saving process for refining 1-butene according to claim 1, characterized in that: and when the 1-butene returns to the tower kettle of the light component removal tower, the temperature is 60-85 ℃, and the pressure is 0.75-1.25 MPaG.
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