CN210796296U - Propylene carbonate preparation facilities based on carbon dioxide raw materials - Google Patents
Propylene carbonate preparation facilities based on carbon dioxide raw materials Download PDFInfo
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- CN210796296U CN210796296U CN201921064694.XU CN201921064694U CN210796296U CN 210796296 U CN210796296 U CN 210796296U CN 201921064694 U CN201921064694 U CN 201921064694U CN 210796296 U CN210796296 U CN 210796296U
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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Abstract
The utility model relates to a propylene carbonate preparation facilities field discloses a propylene carbonate preparation facilities based on carbon dioxide raw materials, including business turn over material subassembly, reaction subassembly, separation subassembly, distillation subassembly, condensation subassembly and propylene carbonate finished product holding vessel, business turn over material subassembly includes that carbon dioxide lets in the pipe, the catalyst lets in pipe, epoxypropane inflow pipe and heat exchanger, is provided with the first heat transfer cavity and the second heat transfer cavity of mutual isolation in the heat exchanger, and the epoxypropane inflow pipe communicates with first heat transfer cavity. The utility model greatly improves the purity of the propylene carbonate finished product through the separation and purification of the reaction mixture by the separator group and the distillation component; furthermore, the initial temperature of propylene oxide before entering the reaction tower is increased and the initial temperature of the reaction mixture before condensation is decreased by recycling the reaction heat, thereby shortening the heating time of propylene oxide and the cooling time of the reaction mixture and reducing the energy consumption.
Description
Technical Field
The utility model relates to a propylene carbonate preparation facilities field especially relates to a propylene carbonate preparation facilities based on carbon dioxide raw materials.
Background
Since the industrial revolution, fossil fuels have been used in large quantities, and carbon dioxide, which is considered to be a greenhouse gas and is one of the major sources of global warming, is emitted excessively during the combustion process thereof, so that it is important to reduce the emission of carbon dioxide or to comprehensively utilize carbon dioxide for the alleviation of global warming.
The conversion of carbon dioxide into organic carbonate is one of effective ways for reducing carbon dioxide emission, at present, mixed gas and liquid comprise three major types of cyclic carbonate, acyclic carbonate and polycarbonate, wherein the synthesis of propylene carbonate from carbon dioxide and propylene oxide is a field with wide application, and the generated propylene carbonate product is not only a solvent with excellent performance, but also an important organic chemical product and has wide application in the fields of batteries, textiles, printing and dyeing and polymer synthesis.
Traditional propylene carbonate preparation facilities includes reaction tower and cooler, lets in carbon dioxide, catalyst and epoxypropane in the reaction tower, and carbon dioxide and epoxypropane synthesize propylene carbonate under the catalysis of catalyst, obtain the propylene carbonate product, then directly arrange into the cooler and cool down. However, the propylene carbonate product prepared by the propylene carbonate preparation device contains carbon dioxide, a catalyst and propylene oxide besides propylene carbonate, so that the propylene carbonate has low purity. Moreover, after the cycloaddition reaction, the temperature of the propylene carbonate product is very high, and the reaction mixture is directly cooled, so that the cooling time is long and the energy consumption is high.
SUMMERY OF THE UTILITY MODEL
The utility model aims at overcoming the weak point among the prior art, provide an improve propylene carbonate finished product purity, shorten the time of cooling and reduce the energy consumption's propylene carbonate preparation facilities based on carbon dioxide raw materials.
The purpose of the utility model is realized through the following technical scheme:
a propylene carbonate preparation facilities based on carbon dioxide raw materials includes:
the device comprises a feeding and discharging assembly, a heat exchanger and a heat exchanger, wherein the feeding and discharging assembly comprises a carbon dioxide inlet pipe, a catalyst inlet pipe, a propylene oxide inlet pipe and a heat exchanger, a first heat exchange cavity and a second heat exchange cavity which are isolated from each other are arranged in the heat exchanger, and the propylene oxide inlet pipe is communicated with the first heat exchange cavity;
the reaction component comprises a reaction tower and a reaction mixture outflow pipe, the reaction tower comprises an upper end enclosure, a tower body and a lower end enclosure, the upper end enclosure and the lower end enclosure are respectively connected with the tower body, the lower end enclosure is respectively communicated with the carbon dioxide inlet pipe, the catalyst inlet pipe and the first heat exchange cavity, the first end of the reaction mixture outflow pipe is communicated with the upper end enclosure, and the second end of the reaction mixture outflow pipe is communicated with the second heat exchange cavity;
the separation assembly comprises a separator group, a carbon dioxide outflow pipe and a propylene carbonate crude product outflow pipe, the separator group is communicated with the second heat exchange cavity, the top of the separator group is communicated with the carbon dioxide outflow pipe, and the bottom of the separator group is communicated with the first end of the propylene carbonate crude product outflow pipe;
the distillation assembly comprises a distillation tower, a propylene carbonate finished product outflow pipe and a catalyst outflow pipe, wherein the distillation tower is communicated with the second end of the propylene carbonate crude product outflow pipe, the top of the distillation tower is communicated with the first end of the propylene carbonate finished product outflow pipe, and the bottom of the distillation tower is communicated with the catalyst outflow pipe;
the condensation component comprises a condenser and a propylene carbonate finished product circulation pipe, wherein the first end of the condenser is communicated with the second end of the propylene carbonate finished product outflow pipe, and the second end of the condenser is communicated with the first end of the propylene carbonate finished product circulation pipe; and
and the propylene carbonate finished product storage tank is communicated with the second end of the propylene carbonate finished product circulation pipe.
In one embodiment, the feeding and discharging assembly further comprises a carbon dioxide heater disposed on the carbon dioxide inlet pipe.
In one embodiment, the feeding and discharging assembly further comprises a propylene oxide pressurizing pump, and the propylene oxide pressurizing pump is communicated with one end of the propylene oxide inflow pipe, which is far away from the first heat exchange cavity.
In one embodiment, the feeding and discharging assembly further comprises a propylene oxide transition connecting pipe, and the propylene oxide transition connecting pipe is respectively communicated with the lower end enclosure and the first heat exchange cavity.
In one embodiment, the feeding and discharging assembly further comprises a propylene oxide heater, and the propylene oxide heater is arranged on the propylene oxide transition connecting pipe.
In one of them embodiment, the separator group includes first order separator and second grade separator, first order separator with second heat transfer cavity intercommunication, the second grade separator with first order separator intercommunication, first order separator reaches the top of second grade separator respectively with the carbon dioxide outlet pipe intercommunication, the bottom of second grade separator group with the first end intercommunication of propylene carbonate crude product outlet pipe.
In one embodiment, the distillation assembly further comprises a steam generator in communication with the distillation column.
In one embodiment, the separation assembly further comprises a carbon dioxide return pipe, a first end of the carbon dioxide return pipe is communicated with the carbon dioxide outlet pipe, and a second end of the carbon dioxide return pipe is communicated with the carbon dioxide inlet pipe.
In one embodiment, the distillation assembly further comprises a catalyst return pipe, a first end of the catalyst return pipe is communicated with the catalyst outlet pipe, and a second end of the catalyst return pipe is communicated with the catalyst inlet pipe.
In one embodiment, the condensation assembly further comprises a propylene carbonate finished product return pipe, the first end of the propylene carbonate finished product return pipe is communicated with the second end of the condenser, and the second end of the propylene carbonate finished product return pipe is communicated with the distillation tower.
Compared with the prior art, the utility model discloses at least, following advantage has:
1. the utility model separates and purifies the reaction mixture through the separator group and the distillation tower, so that the finished product of the propylene carbonate has good quality, and the purity of the propylene carbonate reaches up to 99 percent; moreover, the initial temperature of the propylene oxide before entering the reaction tower is increased and the initial temperature of the reaction mixture before separation is reduced by recycling the reaction heat, so that the heating time of the propylene oxide and the cooling time of the reaction mixture are shortened, and the energy consumption is further reduced.
2. The utility model discloses with the temperature control of one-level separator at 60 ℃ -80 ℃, carbon dioxide and propylene oxide in the reaction mixture are arranged, again with second grade separator temperature control at 105 ℃ -230 ℃, tetrabutyl ammonium bromide is arranged for only remaining potassium iodide and propylene carbonate in the reaction mixture, so, just can guarantee effectively going on of distillation operation, thereby guarantee the off-the-shelf purity of propylene carbonate.
3. The utility model discloses a carbon dioxide back flow and catalyst back flow come to retrieve carbon dioxide and catalyst respectively to reduce material cost and reduce greenhouse gas and discharge.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are required to be used in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some embodiments of the present invention, and therefore should not be considered as limiting the scope, and for those skilled in the art, other related drawings can be obtained according to the drawings without inventive efforts.
FIG. 1 is a schematic structural diagram of a propylene carbonate production apparatus based on a carbon dioxide raw material according to an embodiment of the present invention;
fig. 2 is a schematic structural diagram of a propylene carbonate production apparatus based on a carbon dioxide raw material according to an embodiment of the present invention.
Detailed Description
In order to facilitate understanding of the present invention, the present invention will be described more fully hereinafter with reference to the accompanying drawings. The preferred embodiments of the present invention are shown in the drawings. The invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete.
It will be understood that when an element is referred to as being "secured to" another element, it can be directly on the other element or intervening elements may also be present. When an element is referred to as being "connected" to another element, it can be directly connected to the other element or intervening elements may also be present. The terms "vertical," "horizontal," "left," "right," and the like as used herein are for illustrative purposes only and do not represent the only embodiments.
Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terminology used herein in the description of the invention is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. As used herein, the term "and/or" includes any and all combinations of one or more of the associated listed items.
In one embodiment, referring to fig. 1, an apparatus 10 for preparing propylene carbonate based on carbon dioxide raw material includes a feeding and discharging assembly 110, a reaction assembly 120, a separation assembly 130, a distillation assembly 140, a condensation assembly 150, and a storage tank 160 for a finished product of propylene carbonate. The feeding and discharging assembly 110 comprises a carbon dioxide inlet pipe 111, a catalyst inlet pipe 112, a propylene oxide inlet pipe 113 and a heat exchanger 114, wherein a first heat exchange cavity and a second heat exchange cavity which are isolated from each other are arranged in the heat exchanger 114, and the propylene oxide inlet pipe 113 is communicated with the first heat exchange cavity. The reaction assembly 120 comprises a reaction tower 121 and a reaction mixture outflow pipe 122, the reaction tower 121 comprises an upper seal head, a tower body and a lower seal head, the upper seal head and the lower seal head are respectively connected with the tower body, the lower seal head is respectively communicated with the carbon dioxide inlet pipe 111, the catalyst inlet pipe 112 and the first heat exchange cavity, the first end of the reaction mixture outflow pipe 122 is communicated with the upper seal head, and the second end of the reaction mixture outflow pipe 122 is communicated with the second heat exchange cavity. The separation assembly 130 comprises a separator group 131, a carbon dioxide outflow pipe 132 and a crude propylene carbonate outflow pipe 133, the separator group 131 is communicated with the second heat exchange cavity, the top of the separator group 131 is communicated with the carbon dioxide outflow pipe 132, and the bottom of the separator group 131 is communicated with the first end of the crude propylene carbonate outflow pipe 133. The distillation assembly 140 comprises a distillation tower 141, a propylene carbonate finished product outflow pipe 142 and a catalyst outflow pipe 143, wherein the distillation tower 141 is communicated with the second end of the propylene carbonate crude product outflow pipe 133, the top of the distillation tower 141 is communicated with the first end of the propylene carbonate finished product outflow pipe 142, and the bottom of the distillation tower 141 is communicated with the catalyst outflow pipe 143. The condensation assembly 150 comprises a condenser 151 and a propylene carbonate finished product circulation pipe 152, wherein a first end of the condenser 151 is communicated with a second end of the propylene carbonate finished product outflow pipe 142, and a second end of the condenser 151 is communicated with a first end of the propylene carbonate finished product circulation pipe 152. The propylene carbonate product storage tank 160 is in communication with a second end of the propylene carbonate product flow conduit 152.
The apparatus 10 for producing propylene carbonate based on a carbon dioxide raw material as described above will be explained: taking potassium iodide as a catalyst and polyethylene glycol and tetrabutylammonium bromide as co-catalysts as examples, the propylene oxide inflow pipe 113 introduces propylene oxide to be reacted into a first heat exchange cavity of the heat exchanger 114, the second heat exchange cavity is used for containing a reaction mixture, and the propylene oxide in the first heat exchange cavity exchanges heat with the reaction mixture in the second heat exchange cavity. After the propylene oxide absorbs the heat of the reaction mixture, the propylene oxide is introduced into the reaction tower 121, carbon dioxide and a catalyst are respectively introduced through a carbon dioxide introduction pipe 111 and a catalyst introduction pipe 112, and the temperature and the pressure of the reaction tower 121 are increased to 130-150 ℃ and 1.5-1.8 MPa by heating and pressurizing the reaction tower. In this case, carbon dioxide is in the vapor phase and propylene oxide, catalyst and cocatalyst are in the liquid phase. The carbon dioxide and the propylene oxide are catalyzed by the catalyst and the cocatalyst to synthesize the propylene carbonate, and a reaction mixture is obtained. Then, the reaction mixture is introduced into the separator group 131 through the reaction mixture outflow pipe 122, and the temperature of the separator is lowered to 105 to 150 ℃ to perform a gas-liquid separation operation on the reaction mixture. At this time, the propylene oxide and tetrabutylammonium bromide are converted from the liquid phase to the gas phase, and are discharged from the carbon dioxide outflow pipe 132 together with carbon dioxide as a mixed gas. The propylene carbonate, the catalyst and the polyethylene glycol are still in liquid phase and are used together as ester-containing mixed liquid, and the mixed liquid is introduced into the distillation tower 141 from a propylene carbonate crude product outflow pipe 133. Then, the distillation column 141 is heated and pressurized to a temperature of 230 to 240 ℃ and a pressure of 0.01 to 0.05MPa, and the ester-containing mixed liquid is distilled. The catalyst and polyethylene glycol remain in liquid phase and are used together as a circulating catalytic concentrate, which remains in the distillation column 141. The boiling point of the propylene carbonate at normal pressure is 240 ℃, the propylene carbonate is converted into gas phase under the high-temperature and high-pressure condition, and the gas phase is used as a propylene carbonate finished product and is introduced into a condenser 151 from a propylene carbonate finished product outflow pipe 142. Then, the finished product of propylene carbonate is condensed by a condenser 151, and the temperature of the finished product of propylene carbonate is reduced to normal temperature, so that the finished product of propylene carbonate is converted from gas phase to liquid phase. Then, the propylene carbonate finished product circulation pipe 152 leads the condensed propylene carbonate finished product into the propylene carbonate finished product storage tank 160 for storage. Thus, the propylene carbonate finished product with the purity of more than 99 percent can be obtained.
In addition, it should be noted that the heat exchange between the propylene oxide and the reaction mixture is performed by the heat exchanger 114, so that the initial temperature of the propylene oxide before entering the reaction tower 121 is increased and the initial temperature of the reaction mixture before separation is decreased by recycling the reaction heat, thereby shortening the heating time of the propylene oxide and the cooling time of the reaction mixture, and further reducing the energy consumption.
Further, referring to fig. 1, the feeding and discharging assembly 110 further includes a carbon dioxide heater 115, and the carbon dioxide heater 115 is disposed on the carbon dioxide inlet pipe 111. The temperature of the carbon dioxide is raised to 130 to 150 ℃ by the carbon dioxide heater 115.
Further, referring to fig. 1, the feeding and discharging assembly 110 further includes a propylene oxide pressurizing pump 116, and the propylene oxide pressurizing pump 116 is communicated with an end of the propylene oxide inflow pipe 113 away from the first heat exchange cavity. The propylene oxide pressure pump 116 can increase the pressure of the propylene oxide fluid to avoid the propylene oxide fluid from failing to enter the reaction column 121 due to insufficient pressure, and can control the flow rate of the propylene oxide fluid to control the amount of the propylene oxide fluid used in the reaction.
Further, referring to fig. 1, the feeding and discharging assembly 110 further includes a propylene oxide transition connection pipe 117, and the propylene oxide transition connection pipe 117 is respectively communicated with the lower head and the first heat exchange cavity. The feeding and discharging assembly 110 further comprises a propylene oxide heater 118, and the propylene oxide heater 118 is disposed on the propylene oxide transition connecting pipe 117. The temperature of propylene oxide after heat exchange is raised to 130 to 150 ℃ by the propylene oxide heater 118.
Further, referring to fig. 1, the separator set 131 includes a first separator 1311, a second separator 1312, and a tetrabutylammonium bromide outflow pipe 1313. The primary separator 1311 is communicated with the second heat exchange cavity, the secondary separator 1312 is communicated with the primary separator 1311, the top of the primary separator 1311 is communicated with the carbon dioxide outflow pipe 132, the first end of the tetrabutylammonium bromide outflow pipe 1313 is communicated with the top of the secondary separator 1312, the second end of the tetrabutylammonium bromide outflow pipe 1313 is communicated with the carbon dioxide outflow pipe 132, and the bottom of the group 131 of the secondary separators 1312 is communicated with the first end of the crude propylene carbonate outflow pipe 133. In the case where potassium iodide is used as a catalyst and polyethylene glycol and tetrabutylammonium bromide are used as co-catalysts, the temperature of the primary separator 1311 is controlled to 60 ℃ to 80 ℃, and carbon dioxide and propylene oxide in the reaction mixture are discharged through the carbon dioxide outflow pipe 132. The temperature of the second separator 1312 is controlled to 105 ℃ to 150 ℃, and tetrabutylammonium bromide is discharged through a tetrabutylammonium bromide outflow pipe 1313, so that only potassium iodide, polyethylene glycol and propylene carbonate remain in the reaction mixture. Therefore, the effective operation of distillation operation can be ensured, and the purity of the propylene carbonate finished product is ensured.
Further, referring to fig. 1, the distillation assembly 140 further includes a steam generator 144, and the steam generator 144 is in communication with the distillation tower 141. The steam generator 144 supplies high-temperature steam to the distillation column 141 to raise the temperature of the distillation column 141 to 230 to 240 ℃.
Further, referring to fig. 1, the separation assembly 130 further includes a carbon dioxide return pipe 134, a first end of the carbon dioxide return pipe 134 is communicated with the carbon dioxide outlet pipe 132, and a second end of the carbon dioxide return pipe 134 is communicated with the carbon dioxide inlet pipe 111. It should be noted that the carbon dioxide return pipe 134 can recover carbon dioxide and propylene oxide into the reaction tower 121, thereby reducing the cost of carbon dioxide and reducing greenhouse gas emissions.
Further, the distillation assembly 140 further includes a catalyst return pipe 145, a first end of the catalyst return pipe 145 is communicated with the catalyst outflow pipe 143, and a second end of the catalyst return pipe 145 is communicated with the catalyst introduction pipe 112. It should be noted that catalyst return line 145 can return the catalyst and a portion of the co-catalyst to reaction tower 121, thereby reducing the catalyst cost.
Further, referring to fig. 1, the condensing assembly 150 further includes a finished propylene carbonate return pipe 153, a first end of the finished propylene carbonate return pipe 153 is communicated with a second end of the condenser 151, and a second end of the finished propylene carbonate return pipe 153 is communicated with the distillation tower 141. It should be noted that the temperature in the distillation tower 141 is 230-240 ℃, and the reaction temperature required by the reaction tower 121 is 130-150 ℃, so the catalyst and part of the cocatalyst need to be cooled before being recycled and introduced into the reaction tower 121, compared with the method of adding a condenser 151 to cool the catalyst and part of the cocatalyst, the utility model discloses a return a part of the condensed propylene carbonate finished product to the distillation tower 141 through the propylene carbonate finished product return pipe 153, exchange heat with the catalyst and part of the cocatalyst in the distillation tower 141, so that the temperature of the catalyst and part of the cocatalyst is reduced to 130-150 ℃, and then the catalyst and part of the cocatalyst is recycled to the reaction tower 121, so that the function of condensing the catalyst and part of the cocatalyst before being recycled is achieved, and simultaneously, the equipment cost and the equipment floor area can be reduced.
Compared with the prior art, the utility model discloses at least, following advantage has:
1. the utility model separates and purifies the reaction mixture through the separator group 131 and the distillation tower 141, so that the finished product of the propylene carbonate has good quality, and the purity of the propylene carbonate reaches up to 99 percent; furthermore, the initial temperature of propylene oxide before entering the reaction tower 121 is increased and the initial temperature of the reaction mixture before separation is decreased by recycling the reaction heat, thereby shortening the heating time of propylene oxide and the cooling time of the reaction mixture and further reducing the energy consumption.
2. The utility model discloses with the temperature control of primary separator 1311 at 60 ℃ -80 ℃, carbon dioxide and propylene oxide in the reaction mixture are arranged, again with secondary separator 1312 temperature control at 105 ℃ -230 ℃, tetrabutyl ammonium bromide is arranged for only remaining potassium iodide and propylene carbonate in the reaction mixture, so, just can guarantee effectively going on of distillation operation, thereby guarantee the off-the-shelf purity of propylene carbonate.
3. The utility model discloses a carbon dioxide and catalyst are retrieved respectively to carbon dioxide back flow 134 and catalyst back flow 145 to reduce material cost and reduce greenhouse gas and discharge.
The above-mentioned embodiments only represent some embodiments of the present invention, and the description thereof is specific and detailed, but not to be construed as limiting the scope of the present invention. It should be noted that, for those skilled in the art, without departing from the spirit of the present invention, several variations and modifications can be made, which are within the scope of the present invention. Therefore, the protection scope of the present invention should be subject to the appended claims.
Claims (10)
1. The utility model provides a propylene carbonate preparation facilities based on carbon dioxide raw materials which characterized in that includes:
the device comprises a feeding and discharging assembly, a heat exchanger and a heat exchanger, wherein the feeding and discharging assembly comprises a carbon dioxide inlet pipe, a catalyst inlet pipe, a propylene oxide inlet pipe and a heat exchanger, a first heat exchange cavity and a second heat exchange cavity which are isolated from each other are arranged in the heat exchanger, and the propylene oxide inlet pipe is communicated with the first heat exchange cavity;
the reaction component comprises a reaction tower and a reaction mixture outflow pipe, the reaction tower comprises an upper end enclosure, a tower body and a lower end enclosure, the upper end enclosure and the lower end enclosure are respectively connected with the tower body, the lower end enclosure is respectively communicated with the carbon dioxide inlet pipe, the catalyst inlet pipe and the first heat exchange cavity, the first end of the reaction mixture outflow pipe is communicated with the upper end enclosure, and the second end of the reaction mixture outflow pipe is communicated with the second heat exchange cavity;
the separation assembly comprises a separator group, a carbon dioxide outflow pipe and a propylene carbonate crude product outflow pipe, the separator group is communicated with the second heat exchange cavity, the top of the separator group is communicated with the carbon dioxide outflow pipe, and the bottom of the separator group is communicated with the first end of the propylene carbonate crude product outflow pipe;
the distillation assembly comprises a distillation tower, a propylene carbonate finished product outflow pipe and a catalyst outflow pipe, wherein the distillation tower is communicated with the second end of the propylene carbonate crude product outflow pipe, the top of the distillation tower is communicated with the first end of the propylene carbonate finished product outflow pipe, and the bottom of the distillation tower is communicated with the catalyst outflow pipe;
the condensation component comprises a condenser and a propylene carbonate finished product circulation pipe, wherein the first end of the condenser is communicated with the second end of the propylene carbonate finished product outflow pipe, and the second end of the condenser is communicated with the first end of the propylene carbonate finished product circulation pipe; and
and the propylene carbonate finished product storage tank is communicated with the second end of the propylene carbonate finished product circulation pipe.
2. The apparatus for preparing propylene carbonate based on carbon dioxide raw material according to claim 1, wherein the feeding and discharging assembly further comprises a carbon dioxide heater, and the carbon dioxide heater is arranged on the carbon dioxide inlet pipe.
3. The apparatus for preparing propylene carbonate based on carbon dioxide raw material according to claim 1, wherein the feeding and discharging assembly further comprises a propylene oxide pressurizing pump, and the propylene oxide pressurizing pump is communicated with one end of the propylene oxide inflow pipe, which is far away from the first heat exchange cavity.
4. The apparatus for preparing propylene carbonate based on carbon dioxide raw material according to claim 1, wherein the feeding and discharging assembly further comprises a propylene oxide transition connecting pipe, and the propylene oxide transition connecting pipe is respectively communicated with the lower head and the first heat exchange cavity.
5. The apparatus for preparing propylene carbonate based on carbon dioxide raw material according to claim 4, wherein the feeding and discharging assembly further comprises a propylene oxide heater, and the propylene oxide heater is arranged on the propylene oxide transition connecting pipe.
6. The apparatus of claim 1, wherein the separator group comprises a first-stage separator and a second-stage separator, the first-stage separator is communicated with the second heat exchange cavity, the second-stage separator is communicated with the first-stage separator, the tops of the first-stage separator and the second-stage separator are respectively communicated with the carbon dioxide outflow pipe, and the bottom of the second-stage separator group is communicated with the first end of the crude product outflow pipe of propylene carbonate.
7. The apparatus of claim 1, wherein the distillation assembly further comprises a steam generator in communication with the distillation column.
8. The apparatus for preparing propylene carbonate based on carbon dioxide feedstock as claimed in claim 1, wherein said separation assembly further comprises a carbon dioxide return pipe, a first end of said carbon dioxide return pipe being in communication with said carbon dioxide outlet pipe, a second end of said carbon dioxide return pipe being in communication with said carbon dioxide inlet pipe.
9. The apparatus for preparing propylene carbonate based on carbon dioxide feedstock as claimed in claim 1, wherein said distillation assembly further comprises a catalyst return pipe, a first end of said catalyst return pipe being in communication with said catalyst outlet pipe, a second end of said catalyst return pipe being in communication with said catalyst inlet pipe.
10. The apparatus for preparing propylene carbonate based on carbon dioxide as claimed in claim 1, wherein the condensing assembly further comprises a finished propylene carbonate return pipe, a first end of the finished propylene carbonate return pipe is communicated with a second end of the condenser, and a second end of the finished propylene carbonate return pipe is communicated with the distillation tower.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| US20230407715A1 (en) * | 2022-06-21 | 2023-12-21 | Baker Hughes Oilfield Operations Llc | Method and system for managing carbon containing gases |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US20230407715A1 (en) * | 2022-06-21 | 2023-12-21 | Baker Hughes Oilfield Operations Llc | Method and system for managing carbon containing gases |
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