CN216716762U - Device for producing carbon dioxide by adopting two refrigeration working conditions - Google Patents
Device for producing carbon dioxide by adopting two refrigeration working conditions Download PDFInfo
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- CN216716762U CN216716762U CN202221161823.9U CN202221161823U CN216716762U CN 216716762 U CN216716762 U CN 216716762U CN 202221161823 U CN202221161823 U CN 202221161823U CN 216716762 U CN216716762 U CN 216716762U
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Abstract
The utility model belongs to a device for producing carbon dioxide by adopting two refrigeration working conditions; the device comprises a raw material gas pipeline and an ammonia storage device, wherein the raw material gas pipeline is connected with a first rectifying tower, a gas-phase outlet at the top of the first rectifying tower is connected with a first inlet of a first heat exchanger, a first outlet of the first heat exchanger is connected with a first gas-liquid separator, a gas-phase outlet of the first gas-liquid separator is connected with a first inlet of a second heat exchanger, a first outlet of the second heat exchanger is connected with an inlet of a second gas-liquid separator, a liquid-phase outlet of the second gas-liquid separator is connected with a reflux liquid port of the second rectifying tower, and a liquid-phase outlet at the bottom of the second rectifying tower is connected with a product storage tank; the refrigeration system has the characteristics that the refrigeration working condition can be simplified, carbon dioxide can be produced under two refrigeration working conditions on the premise of ensuring low-energy-consumption operation, the operation difficulty is reduced, the investment is saved, and the energy consumption is reduced.
Description
Technical Field
The utility model belongs to the technical field of carbon dioxide production, and particularly relates to a device for producing carbon dioxide by adopting two refrigeration working conditions.
Background
Carbon dioxide (carbon dioxide), a carbon oxide, having the chemical formula of CO2, the chemical formula of 44.0095, is a colorless, tasteless or colorless, odorless gas at normal temperature and pressure, and has a slightly sour taste in its aqueous solution, and can be widely used, and the gaseous carbon dioxide can be used for carbonizing soft drinks, chemical processing, food preservation, inert protection, welding gas and plant growth stimulator in chemical and food processing processes; taking welding gas as an example, the most common welding modes of hoisting equipment are hybrid gas shielded welding and submerged arc automatic welding, wherein carbon dioxide is a common shielding gas for hybrid gas shielded welding. The carbon dioxide gas shielded welding has the greatest characteristic that oxygen in the air can be prevented from contacting with the metal melted at the welding point at high temperature, and the metal in the welding process can be protected from oxidation, so that the carbon dioxide gas shielded welding is one of the most important welding methods for ferrous metal materials. Compared with a common welding mode, the advantages of carbon dioxide gas shielded welding are also obvious, and can be embodied in the following aspects: 1. the welding cost is low, and is only 40-50% of that of rational arc welding and shielded metal arc welding. 2. The production efficiency is high, and the production efficiency is 1-4 times of that of the shielded metal arc welding. 3. The crack resistance of the welding seam is high. The low-hydrogen-content nitrogen content of the welding seam is less. 4. The deformation after welding is small. The angular deformation is five thousandths, and the unevenness is only three thousandths; 5. the welding spatter is small. When an ultra-low carbon alloy welding wire or a flux-cored welding wire is adopted, or Ar is added into CO2, welding spatter can be reduced. 6. The carbon dioxide gas raw material is easy to extract and refine, the preparation difficulty in the welding process is reduced to a great extent, the application range is wider, the operation is simple and convenient, open arc welding can be carried out, all-position welding can be carried out, downward welding can be carried out, the thickness of a workpiece is not limited, and the welding device is friendly to operators.
At present, in order to reduce the energy consumption of carbon dioxide production and realize gradient utilization of cold energy as much as possible, chemical enterprises generally adopt three working condition refrigeration processes, and the refrigeration processes enable one set of carbon dioxide production system to be matched with three ice machines, so that the operation is complex, the ice machines are difficult to adjust when multiple sets of systems operate simultaneously, and energy loss is caused.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a device for producing carbon dioxide by adopting two refrigeration working conditions so as to solve the problems in the background technology.
In order to achieve the purpose, the utility model provides the following technical scheme:
a device for producing carbon dioxide by adopting two refrigeration working conditions comprises a feed gas pipeline and an ammonia storage device, wherein the feed gas pipeline is connected with a raw material inlet at the middle lower part of a first rectifying tower, a gas-phase outlet at the top part of the first rectifying tower is connected with a first inlet of a first heat exchanger, a first outlet of the first heat exchanger is connected with an inlet of a first gas-liquid separator, a gas-phase outlet of the first gas-liquid separator is connected with a first inlet of a second heat exchanger, a first outlet of the second heat exchanger is connected with an inlet of a second gas-liquid separator, a liquid-phase outlet of the second gas-liquid separator is connected with a reflux liquid port of the second rectifying tower, and a liquid-phase outlet at the bottom part of the second rectifying tower is connected with a product storage tank;
the outlet of the ammonia storage device is connected with the liquid ammonia separator, the liquid phase outlet at the bottom of the liquid ammonia separator is respectively connected with the second inlet of the first heat exchanger and the second inlet of the second heat exchanger, and the second outlet of the first heat exchanger is connected with the inlet of the ammonia storage device through the standard working condition ice machine and the evaporative condenser;
and a second outlet of the second heat exchanger is respectively connected with a first reboiler at the lower part of the first rectifying tower and a second reboiler at the lower part of the second rectifying tower through a low-temperature working condition ice machine.
As a further preferred mode of the technical scheme, a gas phase outlet at the top of the liquid ammonia separator is connected with an outlet of the ice machine under the low-temperature working condition; the outlets of the first reboiler and the second reboiler are connected to the liquid phase outlet at the bottom of the liquid ammonia separator.
As a further preferred mode of the present invention, the liquid phase outlet of the first gas-liquid separator is connected to a reflux inlet at the upper part of the first rectifying column.
As a further preferable mode of the present technical solution, a liquid phase outlet at the bottom of the first rectification column is connected to a collection barrel.
As a further preferred aspect of the present invention, a gas phase outlet of the second gas-liquid separator is connected to a tail gas treatment device.
As a further preferable mode of the present technical solution, the gas phase outlet at the top of the second rectifying tower is connected to the gas phase outlet at the top of the first rectifying tower.
As a further preferable mode of the technical scheme, a first throttling valve is arranged between the outlet of the ammonia storage device and the liquid ammonia separator, a second throttling valve is arranged in front of a second inlet of the first heat exchanger, and a third throttling valve is arranged in front of a second inlet of the second heat exchanger.
The device for producing carbon dioxide by adopting two refrigeration working conditions is manufactured according to the scheme, the standard working condition ice machine and the low-temperature working condition ice machine can adopt two refrigeration working conditions, namely-18 ℃/35 ℃ and-27 ℃/35 ℃, a liquid ammonia throttling valve from an ammonia storage device throttles, then liquid ammonia and gas ammonia are obtained through gas-liquid separation, the liquid ammonia is throttled step by step to obtain the gas ammonia as a heat source to enter two reboilers, the gas ammonia is changed into latent heat generated by liquid from gas, and sensible heat generated by supercooling provides a large amount of heat energy for the reboilers, and the generated liquid ammonia can continue throttling to provide cold energy for a system, so that a refrigeration cycle is formed. Meanwhile, the process is simplified, the operation difficulty is reduced, the investment is saved, and the energy consumption is effectively reduced.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
Detailed Description
The technical solution in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention.
As shown in fig. 1, the present invention provides a technical solution: a device for producing carbon dioxide by adopting two refrigeration working conditions comprises a feed gas pipeline 1 and an ammonia storage device 9, wherein the feed gas pipeline 1 is connected with a raw material inlet at the middle lower part of a first rectifying tower 2, a gas-phase outlet at the top part of the first rectifying tower 2 is connected with a first heat exchanger inlet 18 of a first heat exchanger 3, a first heat exchanger outlet 19 is connected with an inlet of a first gas-liquid separator 4, a gas-phase outlet of the first gas-liquid separator 4 is connected with a second heat exchanger first inlet 20 of a second heat exchanger 5, a second heat exchanger first outlet 21 of the second heat exchanger 5 is connected with an inlet of a second gas-liquid separator 6, a liquid-phase outlet of the second gas-liquid separator 6 is connected with a reflux liquid port of a second rectifying tower 7, and a liquid-phase outlet at the bottom part of the second rectifying tower 7 is connected with a product storage tank 8; the outlet of the ammonia storage device 9 is connected with the liquid ammonia separator 10, the liquid phase outlet at the bottom of the liquid ammonia separator 10 is respectively connected with the second inlet 22 of the first heat exchanger 3 and the second inlet 23 of the second heat exchanger 5 of the first heat exchanger 3, and the second outlet 24 of the first heat exchanger is connected with the inlet of the ammonia storage device 9 through the standard working condition ice machine 11 and the evaporative condenser 12; the second outlet 25 of the second heat exchanger is connected with the first reboiler 14 at the lower part of the first rectifying tower 2 and the second reboiler 15 at the lower part of the second rectifying tower 7 through the ice machine 13 under the low temperature condition. In the utility model, the raw material gas with the purity of CO2 being more than or equal to 98 percent and the water content being less than or equal to 1000ppm in the raw material gas pipeline 1 enters a first rectifying tower 2 for rectification, heavy components are removed after rectification, light components enter a first heat exchanger 3 through a top gas-phase outlet of the first rectifying tower 2 for heat exchange and condensation, the light components enter a first gas-liquid separator 4 for gas-liquid separation after condensation, non-condensable gas after gas-liquid separation exchanges heat through a second heat exchanger 5, gas-liquid separation is performed through a second gas-liquid separator 6 after heat exchange, the separated liquid phase flows back into a second rectifying tower 7 for rectification, the rectified heavy components are product liquid, and the product liquid enters a product storage tank 8 through a liquid-phase outlet at the bottom of the second rectifying tower 7; in the process, the ammonia in the ammonia storage device 9 provides cold energy for the first heat exchanger 3 and the second heat exchanger 5 in the system, and provides a heat source for the first reboiler 14 at the lower part of the first rectifying tower 2 and the second reboiler 15 at the lower part of the second rectifying tower 7 so as to ensure the stable operation of the whole system.
In this embodiment, specifically: the gas phase outlet at the top of the liquid ammonia separator 10 is connected with the outlet of the ice machine 13 under the low-temperature working condition; the outlets of the first reboiler 14 and the second reboiler 15 are connected to the liquid phase outlet at the bottom of the liquid ammonia separator 10. In the utility model, the liquefied liquid ammonia which is liquefied by the first reboiler 14 and the second reboiler 15 is mixed with the liquid ammonia which is separated by the liquid ammonia separator 10 and then enters the first heat exchanger 3 and the second heat exchanger 5 to provide cold energy, so that the aims of saving energy, reducing consumption, simplifying the flow and ensuring continuous operation are fulfilled.
In this embodiment, specifically: and a liquid phase outlet of the first gas-liquid separator 4 is connected with a reflux opening at the upper part of the first rectifying tower 2. Liquid phase separated by enterprises through the first gas-liquid separator 4 flows back to the first rectifying tower 2 through a reflux opening at the upper part of the first rectifying tower 2 to be used as rectifying liquid, and the rectification of the raw material gas is realized.
In this embodiment, specifically: and a liquid phase outlet at the bottom of the first rectifying tower 2 is connected with a collecting barrel 16. Heavy components of the feed gas are removed from the feed gas in the first rectifying tower 2, and the feed gas is discharged from a liquid phase outlet at the bottom of the first rectifying tower 2 to a collecting barrel 16 for uniform treatment.
In this embodiment, specifically: the gas phase outlet of the second gas-liquid separator 6 is connected with a tail gas treatment device 17. The gas phase subjected to gas-liquid separation by the second gas-liquid separator 6 is subjected to off-gas treatment by an off-gas treatment device 17.
In this embodiment, specifically: and a gas phase outlet at the top of the second rectifying tower 7 is connected with a gas phase outlet at the top of the first rectifying tower 2.
In this embodiment, specifically: a first throttle valve 26 is arranged between the outlet of the ammonia storage device 9 and the liquid ammonia separator 10, a second throttle valve 27 is arranged in front of the second inlet 22 of the first heat exchanger 3, and a third throttle valve 28 is arranged in front of the second inlet 23 of the second heat exchanger 5.
The working principle of the utility model is as follows: the purity of feed gas CO2 in the feed gas pipeline 1 is more than or equal to 98 percent, the water content is less than or equal to 1000ppm, other components are oxygen, nitrogen, methane and the like, the pressure is 25-30 barA, the temperature is normal temperature, the feed gas enters the first rectifying tower 2 from a feed inlet at the middle lower part of the first rectifying tower 2, mass transfer and heat transfer are carried out on the feed gas and a rectifying liquid in a reflux port from the upper part of the first rectifying tower 2, heavy components in the feed gas are liquefied and continuously accumulated in the first rectifying tower 2, light components enter the first heat exchanger 3 from a gas phase outlet at the top of the first rectifying tower 2 and a first inlet 18 of the first heat exchanger to be cooled to-13 ℃ to-17 ℃, a large amount of carbon dioxide is liquefied in the cooling process, the gas phase is changed into a gas-liquid mixed state, and the gas-liquid separation is carried out in the first gas-liquid separator 4; the carbon dioxide liquid with higher concentration obtained by separation enters the first rectifying tower 2 through a reflux opening at the upper part of the first rectifying tower 2 to be used as a rectifying liquid; the separated non-condensable gas enters the second heat exchanger 5 through a first inlet 20 of the second heat exchanger 5 to be cooled to minus 20 ℃ to minus 27 ℃, a small amount of carbon dioxide is liquefied and is changed into a gas-liquid mixed state from a gas phase, then the gas-liquid mixed state enters the second gas-liquid separator 6 to be subjected to gas-liquid separation, carbon dioxide liquid with higher concentration obtained through separation enters the second rectifying tower 7 through a liquid phase outlet of the second gas-liquid separator 6 and a reflux liquid port of the second rectifying tower 7 to be rectified, the rectified heavy components are carbon dioxide product liquid, the carbon dioxide product liquid enters a product storage tank 8 through a liquid phase outlet at the bottom of the second rectifying tower 7, and the purity of the carbon dioxide product liquid is more than 99.999%; in the process, the continuously accumulated heavy components in the first rectifying tower 2 are waste liquid which enters the collecting barrel 16 through the liquid phase outlet at the bottom of the first rectifying tower 2, and the gas phase separated in the second gas-liquid separator 6 enters the tail gas treatment device 17 through the gas phase outlet of the second gas-liquid separator 6 for tail gas treatment; the gas phase in the second rectifying tower 7 enters the first heat exchanger 3 again through the first inlet 18 of the first heat exchanger to repeat the steps; the pressure of liquid ammonia in the ammonia storage device 9 is 7-15 barA, throttling is carried out to 3-5 bar through a first throttling valve 26, then the liquid ammonia enters a liquid ammonia separator 10 for gas-liquid separation, ammonia liquid after gas-liquid separation is converged with liquid ammonia from the outlets of a first reboiler 14, a second reboiler 15 and a low-temperature working condition ice machine 13 through a liquid phase outlet at the bottom of the liquid ammonia separator 10 and then is divided into two parts, one part of the ammonia liquid enters a first heat exchanger 3 through a second inlet 22 of the first heat exchanger after being throttled to 1.9-2.3 barA through a second throttling valve 27 to provide cold energy, the cold energy is exchanged with gas phases from a first rectifying tower 2 and a second rectifying tower 7, and the liquid ammonia after heat exchange is gasified and liquefied through a standard working condition ice machine 11 and an evaporative condenser 12 and then enters the ammonia storage device 9 again for recycling; the pressure of the gas ammonia after entering the standard working condition ice machine 11 is 7-15 barA; and the other part of liquid ammonia can be throttled by a second throttling valve 27 and then throttled by a third throttling valve 28 (or directly throttled by the third throttling valve 28), so that the pressure is throttled to 1.2-1.7 barA, then the liquid ammonia enters the second heat exchanger 5 through a second inlet 23 of the second heat exchanger 5 to exchange heat, the liquid ammonia is gasified after the heat exchange, the gasified liquid ammonia enters the ice machine 13 under the low-temperature working condition, the ammonia discharged from the ice machine 13 under the low-temperature working condition is divided into two parts, one part of the ammonia enters a first reboiler 14 to be used as a reboiling heat source of the first rectifying tower 2, the other part of the ammonia enters a second reboiler 15 to be used as a reboiling heat source of the second rectifying tower 7, and the liquefied liquid ammonia serving as the heat source is merged with the liquid ammonia in a liquid phase outlet at the bottom of the liquid ammonia separator 10 to be used as a cold source of the first heat exchanger 3 and the second heat exchanger 5 again. The structure is simple, the flow design is reasonable, two refrigeration working conditions can be adopted by the standard working condition ice machine 11 and the low-temperature working condition ice machine 13, namely-18 ℃/35 ℃ and-27 ℃/35 ℃, liquid ammonia from the ammonia storage device 9 is throttled by the first throttle valve 26, then gas-liquid separation is carried out by the liquid ammonia separator 10 to obtain liquid ammonia and gas ammonia, the liquid ammonia is throttled step by step to obtain-18 ℃ and-27 ℃, the gas ammonia is used as a heat source to enter a reboiler of a rectifying tower, latent heat generated by the gas ammonia changing from gas state to liquid state and sensible heat generated by supercooling provide a large amount of heat energy for the reboiler, the generated liquid ammonia can continue throttling to provide cold energy for the system, thereby forming refrigeration cycle, compared with the prior art, one high-temperature working condition ice machine is reduced, electricity is saved, and the cold energy supplement of a condenser is reduced by absorbing reboiling, further saving energy and reducing consumption.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the utility model, the scope of which is defined in the appended claims and their equivalents.
Claims (7)
1. The utility model provides an adopt two kinds of refrigeration operating mode production carbon dioxide's device, includes feed gas pipeline (1) and ammonia storage ware (9), its characterized in that: the feed gas pipeline (1) is connected with a raw material inlet at the middle lower part of the first rectifying tower (2), a gas-phase outlet at the top part of the first rectifying tower (2) is connected with a first heat exchanger first inlet (18) of the first heat exchanger (3), a first heat exchanger first outlet (19) is connected with an inlet of the first gas-liquid separator (4), a gas-phase outlet of the first gas-liquid separator (4) is connected with a second heat exchanger first inlet (20) of the second heat exchanger (5), a second heat exchanger first outlet (21) of the second heat exchanger (5) is connected with an inlet of the second gas-liquid separator (6), a liquid-phase outlet of the second gas-liquid separator (6) is connected with a reflux liquid port of the second rectifying tower (7), and a liquid-phase outlet at the bottom part of the second rectifying tower (7) is connected with a product storage tank (8);
an outlet of the ammonia storage device (9) is connected with a liquid ammonia separator (10), a liquid phase outlet at the bottom of the liquid ammonia separator (10) is respectively connected with a second inlet (22) of a first heat exchanger of the first heat exchanger (3) and a second inlet (23) of a second heat exchanger of the second heat exchanger (5), and a second outlet (24) of the first heat exchanger is connected with an inlet of the ammonia storage device (9) through an ice machine (11) under standard working conditions and an evaporative condenser (12);
and a second outlet (25) of the second heat exchanger is respectively connected with a first reboiler (14) at the lower part of the first rectifying tower (2) and a second reboiler (15) at the lower part of the second rectifying tower (7) through a low-temperature working condition ice machine (13).
2. The apparatus of claim 1, wherein the apparatus is configured to produce carbon dioxide using two refrigeration regimes: a gas phase outlet at the top of the liquid ammonia separator (10) is connected with an outlet of the ice maker (13) under the low-temperature working condition; the outlets of the first reboiler (14) and the second reboiler (15) are connected to the liquid phase outlet at the bottom of the liquid ammonia separator (10).
3. The apparatus of claim 1, wherein the apparatus is configured to produce carbon dioxide using two refrigeration regimes: and a liquid phase outlet of the first gas-liquid separator (4) is connected with a reflux opening at the upper part of the first rectifying tower (2).
4. A device for producing carbon dioxide using two refrigeration regimes according to claim 1 or claim 3, wherein: and a liquid phase outlet at the bottom of the first rectifying tower (2) is connected with a collecting barrel (16).
5. The apparatus of claim 1, wherein the apparatus is configured to produce carbon dioxide using two refrigeration regimes: and a gas phase outlet of the second gas-liquid separator (6) is connected with a tail gas treatment device (17).
6. The apparatus of claim 1, wherein the apparatus is configured to produce carbon dioxide using two refrigeration regimes: and a gas phase outlet at the top of the second rectifying tower (7) is connected with a gas phase outlet at the top of the first rectifying tower (2).
7. The apparatus of claim 1, wherein the apparatus is configured to produce carbon dioxide using two refrigeration regimes: a first throttling valve (26) is arranged between the outlet of the ammonia storage device (9) and the liquid ammonia separator (10), a second throttling valve (27) is arranged in front of a second inlet (22) of the first heat exchanger (3), and a third throttling valve (28) is arranged in front of a second inlet (23) of the second heat exchanger (5).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221161823.9U CN216716762U (en) | 2022-05-16 | 2022-05-16 | Device for producing carbon dioxide by adopting two refrigeration working conditions |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221161823.9U CN216716762U (en) | 2022-05-16 | 2022-05-16 | Device for producing carbon dioxide by adopting two refrigeration working conditions |
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| CN216716762U true CN216716762U (en) | 2022-06-10 |
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| CN202221161823.9U Active CN216716762U (en) | 2022-05-16 | 2022-05-16 | Device for producing carbon dioxide by adopting two refrigeration working conditions |
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| CN (1) | CN216716762U (en) |
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- 2022-05-16 CN CN202221161823.9U patent/CN216716762U/en active Active
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