CN212680522U - CO 2-containing extraction and refining system in carbonate production tail gas - Google Patents
CO 2-containing extraction and refining system in carbonate production tail gas Download PDFInfo
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- CN212680522U CN212680522U CN202020751692.4U CN202020751692U CN212680522U CN 212680522 U CN212680522 U CN 212680522U CN 202020751692 U CN202020751692 U CN 202020751692U CN 212680522 U CN212680522 U CN 212680522U
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Abstract
The invention provides a method for treating CO in tail gas2CO is contained in the extracted carbonic ester production tail gas2The extraction and refining system comprises a compression precooling system and CO which are sequentially connected in series2An extraction and refining system and a discharge system; wherein, the compression pre-cooling system pre-cools and compresses the feed gas or/and the condensate and then discharges the pre-cooled and compressed feed gas and/or condensate to CO2An extraction and refining system, the CO2The extraction refining system carries out rectification separation on the precooled feed gas or/and condensate to obtain finished product CO2(ii) a By CO2The tail gas and the residual liquid discharged after the rectification of the extraction and refining system enterInto the exhaust system.
Description
Technical Field
The invention relates to the technical field of tail gas treatment in carbonate production, in particular to a method for treating CO-containing tail gas in carbonate production2An extraction and refining system.
Background
In a carbonate production system, the off-gas produced in its production contains a large amount of CO2High pollution and toxic gas, and CO in tail gas2Etc. are common industrial raw materials, and thus, for example, CO in exhaust gas thereof2Is subjected to extractionThe problem of tail gas emission pollution can be reduced, and economic benefits can be brought to production enterprises, so that the design provides a CO-containing material2CO of industrial tail gas2A refining and extracting system.
Disclosure of Invention
The invention aims to overcome the defects of the prior art, meet the practical requirements and provide a carbonic ester production tail gas containing CO2An extraction and refining system.
In order to realize the purpose of the invention, the technical scheme adopted by the invention is as follows:
discloses a carbonic ester production tail gas containing CO2The extraction and refining system comprises a compression precooling system and CO which are sequentially connected in series2An extraction and refining system and a discharge system; wherein, the compression pre-cooling system pre-cools and compresses the feed gas or/and the condensate and then discharges the pre-cooled and compressed feed gas and/or condensate to CO2An extraction and refining system, the CO2The extraction refining system carries out rectification separation on the precooled feed gas or/and condensate to obtain finished product CO2(ii) a By CO2And tail gas and residual liquid discharged after rectification by the extraction and refining system enter the discharge system.
The compression precooling system comprises a precooler, a carbon dioxide compressor front separating tank, a carbon dioxide compressor, a carbon dioxide rear cooler, a carbon dioxide rear separating tank, a carbon dioxide buffer tank and a carbon dioxide blower which are connected in series, wherein:
the upstream gas enters the carbon dioxide buffer tank, and the carbon dioxide buffer tank enters the precooler after being pressurized by a carbon dioxide blower; the outlet of the precooler is connected with a front separation tank of the carbon dioxide compressor, an exhaust port at the top of the front separation tank of the carbon dioxide compressor is divided into two paths, wherein one path is connected with a discharge system, the other path is connected with an air inlet of the carbon dioxide compressor, and a liquid outlet at the bottom of the front separation tank of the carbon dioxide compressor is a residual liquid discharge port;
the exhaust port of the carbon dioxide compressor is connected with the air inlet of the carbon dioxide aftercooler, the exhaust port at the top of the carbon dioxide aftercooler enters the air inlet of the carbon dioxide afterseparating tank, and the exhaust port at the top of the carbon dioxide aftercooler is connected with the air inlet of the carbon dioxide afterseparating tankA condensate discharge port at the bottom of the carbon dioxide rear separation tank is connected with the carbon dioxide compressor front separation tank, and an exhaust port at the top of the carbon dioxide rear separation tank is connected with CO2The extraction and refining system is connected, and the gas discharged from the carbon dioxide post-separation tank enters the CO2Rectifying in an extraction and refining system.
The CO is2The extraction and refining system comprises a heavy component removing tower, a light component removing tower, a heavy component removing separation tank, a heavy component removing condenser, a light component removing separation tank and a light component removing condenser;
the carbon dioxide enters a heavy component removal tower from an exhaust port at the top of the separation tank for heavy component removal treatment, wherein heavy component kettle liquid enters a precooler through a liquid discharge pipe at the bottom, light components enter a heavy component removal condenser through an exhaust pipe for condensation and then enter the heavy component removal separation tank, and a liquid discharge port at the bottom of the heavy component removal separation tank is connected with an inlet at the top of the heavy component removal tower;
the light components treated by the heavy component removal separation tank and the light components rectified by the light component removal tower enter a light component removal condenser through an exhaust port at the top of the light component removal tower to be condensed and then enter the light component removal separation tank together, the condensed liquid treated by the light component removal separation tank enters the light component removal tower again through a liquid discharge pipe to be rectified, and the heavy component kettle liquid rectified by the light component removal tower is condensed into CO through a cooler to be condensed2Putting the finished product into a storage tank;
the light component gas treated by the light component removing and separating tank is discharged from an exhaust port at the top of the light component removing and separating tank and enters an inlet of a first heat exchange tube in the precooler, and an outlet of the first heat exchange tube in the precooler is emptied;
and a liquid discharge port at the bottom of the de-weighting tower is connected with an inlet of a second heat transfer pipe in the precooler, an outlet of the second heat transfer pipe is connected with the front separation tank of the carbon dioxide compressor, a liquid discharge port at the bottom of the front separation tank of the carbon dioxide compressor is connected with a discharge system, and an air exhaust port at the top of the front separation tank of the carbon dioxide compressor is connected with a carbon dioxide buffer tank.
The heavy component removal reboiler in the bottom of the heavy component removal tower and the light component removal reboiler in the bottom of the light component removal tower are connected with ammonia gas or/and liquid ammonia in a refrigeration system, and the outlets of the heavy component removal reboiler and the light component removal reboiler are connected with an ammonia low-pressure circulating barrel;
the system also comprises a standard working condition ammonia separating tank, wherein an exhaust port at the top of the ammonia low-pressure circulating barrel is connected with an inlet of the standard working condition ammonia separating tank, an exhaust port at the top of the standard working condition ammonia separating tank is an ammonia gas exhaust port and enters a refrigeration system, a condensate outlet at the bottom of the standard working condition ammonia separating tank is connected with a heat exchange medium pipe inlet of the de-heavy condenser and a first heat exchange medium inlet of the de-light condenser, and a heat exchange medium pipe outlet of the de-heavy condenser and a first heat exchange medium outlet of the de-light condenser are connected with an inlet of the standard working condition ammonia separating tank;
the system is characterized by further comprising a low-pressure ammonia separation tank, a condensate discharge port at the bottom of the standard working condition ammonia separation tank is further connected with an inlet of the low-pressure ammonia separation tank, an exhaust port at the top of the low-pressure ammonia separation tank is an ammonia gas discharge port and enters a refrigeration system, a condensate outlet at the bottom of the low-pressure ammonia separation tank is connected with a second heat exchange medium inlet of the lightness-removing condenser and a heat exchange medium inlet of the subcooler, and a second heat exchange medium outlet of the lightness-removing condenser and a heat exchange medium outlet of the subcooler are connected with an inlet of the low-pressure ammonia separation tank.
Further comprises a compression pre-cooling system and a CO2Extract the refrigerating system that refined system, discharge system provided the energy, refrigerating system includes liquid storage pot, supplementary liquid storage pot, ammonia cooler, low pressure ice maker, standard operating mode ice maker, ammonia evaporative condenser, wherein:
the liquid storage tank is connected with the auxiliary liquid storage tank through a pipeline, and liquid ammonia in the auxiliary liquid storage tank can enter the liquid storage tank; ammonia gas exhaust pipes are arranged at the tops of the liquid storage tank and the auxiliary liquid storage tank and are connected with an inlet of a lightness-removing reboiler in the lightness-removing tower, ammonia gas enters the lightness-removing reboiler through the ammonia gas exhaust pipes, and a liquid ammonia discharge pipe is arranged on the liquid storage tank and is connected with an inlet of the lightness-removing reboiler in the lightness-removing tower;
a liquid ammonia liquid discharge pipe at the bottom of the auxiliary liquid storage tank is divided into two paths, wherein one path is connected with the inlet of a condenser of the low-pressure ice machine, and the other path is connected with the inlet of the condenser of the standard working condition ice machine; the condenser outlet of the low-pressure ice machine and the condenser outlet of the standard working condition ice machine are connected with the air inlet at the top of the auxiliary liquid storage tank; a liquid ammonia outlet of the ammonia evaporative condenser is connected with a liquid ammonia inlet on the auxiliary liquid storage tank;
the ammonia gas discharged from the exhaust port at the top of the ammonia separation tank under the standard working condition passes through the ice maker under the standard working condition and then enters the ammonia gas inlet of the ammonia evaporative condenser together with the ammonia gas exhaust port at the top of the auxiliary liquid storage tank;
the ammonia gas discharged from an exhaust port at the top of the low-pressure ammonia separation tank enters a heat transfer pipe in an ammonia gas cooler after passing through a low-pressure ice maker, the outlet of the heat transfer pipe in the cooler is connected with the inlet of a heavy component removal reboiler in a heavy component removal tower, the inlet of a cooling water pipeline in the ammonia gas cooler is connected with a circulating water main pipe, and the outlet of the cooling water pipeline in the cooler is connected with a circulating water return main pipe;
and the ammonia gas exhaust pipes at the tops of the liquid storage tank and the auxiliary liquid storage tank are also connected with a discharge system.
The discharge system comprises a buffer tank, a tail gas water seal tank and a liquid collecting tank, wherein the buffer tank is provided with a high-pressure gas inlet pipe and is connected with the liquid storage tank and an ammonia gas exhaust pipe at the top of the auxiliary liquid storage tank, liquid discharge ports at the bottoms of the buffer tank and the tail gas water seal tank are connected with the liquid collecting tank, and the exhaust pipe at the top of the buffer tank is connected with a gas inlet on the tail gas water seal tank.
And the liquid outlet at the bottom of the carbon dioxide buffer tank and the liquid outlet at the bottom of the front separation tank of the carbon dioxide compressor are connected with the liquid collection tank, and the liquid collection tank is internally provided with a submerged pump and discharges the liquid in the liquid collection tank.
The invention has the beneficial effects that:
the designed CO-containing2CO of industrial tail gas2The refining and extracting system has simple structure and easy realization, and can treat CO in the tail gas treatment system2The extraction is carried out, the problem of direct emission and pollution of tail gas is solved, and meanwhile, the economic benefit of enterprises can be improved.
Drawings
FIG. 1 is a schematic diagram of a main principle of a compression pre-cooling system according to the present invention;
FIG. 2 shows CO in the present invention2The main principle schematic diagram of the extraction refining system;
FIG. 3 is a schematic diagram of the principal principles of the refrigeration system of the present invention;
fig. 4 is a schematic view of the main principle of the discharge system of the present invention.
Detailed Description
The invention is further illustrated with reference to the following figures and examples:
example 1: CO is contained in carbonic ester production tail gas2An extraction refining system, see fig. 1-4.
Comprises a compression precooling system and CO which are connected in series in sequence2An extraction and refining system and a discharge system; the principle is that the compression precooling system precools and compresses feed gas or/and condensate and then discharges the feed gas or/and condensate to CO2An extraction and refining system, the CO2The extraction refining system carries out rectification separation on the precooled feed gas or/and condensate to obtain finished product CO2(ii) a By CO2And tail gas and residual liquid discharged after rectification by the extraction and refining system enter the discharge system.
Specifically, the compression precooling system comprises a precooler E101, a carbon dioxide compressor front separation tank V201, a carbon dioxide compressor C102, a carbon dioxide after-cooler E102, a carbon dioxide after-separation tank V102, a carbon dioxide buffer tank V105 and a carbon dioxide blower C101 which are connected in series, wherein:
the upstream gas enters the carbon dioxide buffer tank, and the carbon dioxide buffer tank enters the precooler after being pressurized by a carbon dioxide blower; the outlet of the precooler is connected with the front separation tank of the carbon dioxide compressor, the exhaust port at the top of the front separation tank of the carbon dioxide compressor is divided into two paths, one path is connected with the discharge system, the other path is connected with the air inlet of the carbon dioxide compressor, and the liquid outlet at the bottom of the front separation tank of the carbon dioxide compressor is a residual liquid discharge port.
Furthermore, an exhaust port of the carbon dioxide compressor is connected with an air inlet of a carbon dioxide aftercooler, an exhaust port at the top of the carbon dioxide aftercooler enters the air inlet of the carbon dioxide afterseparating tank, and a condensate discharge port at the bottom of the carbon dioxide afterseparating tank is connected with the carbon dioxideThe front separation tank of the compressor is connected, and the exhaust port at the top of the rear separation tank of the carbon dioxide is connected with CO2The extraction and refining system is connected, and the gas discharged from the carbon dioxide post-separation tank enters the CO2Rectifying in an extraction and refining system.
In particular, the CO2The extraction and refining system comprises a heavy component removal tower T101, a light component removal tower T102, a heavy component removal separation tank V103, a heavy component removal condenser E103, a light component removal separation tank V104 and a light component removal condenser E104; and the carbon dioxide post-separation tank enters an exhaust port 1101 at the top of a de-weighting tower for de-weighting treatment, wherein heavy component kettle liquid enters a precooler through a liquid discharge pipe 1102 at the bottom, light components enter a de-weighting separation tank through an exhaust pipe after entering a de-weighting condenser for condensation, and a liquid discharge port at the bottom of the de-weighting separation tank is connected with an inlet at the top of the de-weighting tower to form a cycle.
Further, the light components treated by the heavy component removal separation tank and the light components rectified by the light component removal tower enter a light component removal condenser through an exhaust port at the top of the light component removal tower to be condensed and then enter the light component removal separation tank together, the condensate treated by the light component removal separation tank enters the light component removal tower again through a liquid discharge pipe to be rectified to form a cycle, and the heavy component kettle liquid rectified by the light component removal tower is condensed into CO through a cooler to form a cycle2And putting the finished product into a storage tank.
Further, the light component gas treated by the light component removing and separating tank is discharged from a gas outlet 1103 at the top of the light component removing and separating tank and enters an inlet of a first heat exchange tube in the precooler, and an outlet of the first heat exchange tube in the precooler is emptied.
Further, a liquid outlet 1102 at the bottom of the de-weighting tower is connected with an inlet of a second heat transfer pipe in the precooler, an outlet of the second heat transfer pipe is connected with the front separation tank of the carbon dioxide compressor, a liquid outlet 1903 at the bottom of the front separation tank of the carbon dioxide compressor is connected with a discharge system, and an exhaust port at the top of the front separation tank of the carbon dioxide compressor is connected with a carbon dioxide buffer tank.
Further, in the system, the inlets of the heavy component removal reboiler E106 in the bottom of the heavy component removal column and the light component removal reboiler E107 in the bottom of the light component removal column are connected to ammonia gas or/and liquid ammonia in the refrigeration system, and the outlets of the heavy component removal reboiler E106 and the light component removal reboiler E107 are connected to the ammonia low-pressure circulation barrel V403.
Further, the system comprises a standard working condition ammonia separating tank V404A, wherein an exhaust port at the top of the ammonia low-pressure circulating barrel is connected with an inlet of the standard working condition ammonia separating tank V404A, an exhaust port at the top of the standard working condition ammonia separating tank V404A is an ammonia gas exhaust port 4401 and enters a refrigeration system, a condensate outlet at the bottom of the standard working condition ammonia separating tank is connected with a heat exchange medium pipe inlet of the de-heavy condenser and a first heat exchange medium inlet of the de-light condenser, and a heat exchange medium pipe outlet of the de-heavy condenser and a first heat exchange medium outlet of the de-light condenser are connected with an inlet of the standard working condition ammonia separating tank.
Still include low pressure ammonia knockout drum V405, the condensate discharge port of standard operating mode ammonia knockout drum bottom still with the access connection of this low pressure ammonia knockout drum, low pressure ammonia knockout drum top gas vent 4402 is the ammonia discharge port and gets into refrigerating system, the condensate exit linkage of low pressure ammonia knockout drum bottom the heat transfer medium import of the second heat transfer medium import of lightness-removing condenser and the heat transfer medium import of subcooler, the heat transfer medium exit linkage of the second heat transfer medium export of lightness-removing condenser and subcooler the import of low pressure ammonia knockout drum.
Furthermore, the system also comprises a compression precooling system and CO2The refrigeration system is characterized by comprising a liquid storage tank V402, an auxiliary liquid storage tank V401, an ammonia gas cooler E402, a low-pressure ice machine C402, a standard working condition ice machine C401 and an ammonia evaporative condenser E401, wherein:
the liquid storage tank is connected with the auxiliary liquid storage tank through a pipeline 4012, and liquid ammonia in the auxiliary liquid storage tank can enter the liquid storage tank; the top of the liquid storage tank and the auxiliary liquid storage tank is provided with an ammonia gas exhaust pipe 4102 and is connected with an inlet of a lightness-removing reboiler in the lightness-removing tower, ammonia gas enters the lightness-removing reboiler through the ammonia gas exhaust pipe, and the liquid storage tank is provided with a liquid ammonia discharge pipe 4101 and is connected with an inlet of the lightness-removing reboiler in the lightness-removing tower.
A liquid ammonia liquid discharge pipe at the bottom of the auxiliary liquid storage tank is divided into two paths, wherein one path is connected with the inlet of a condenser of the low-pressure ice machine, and the other path is connected with the inlet of the condenser of the standard working condition ice machine; the condenser outlet of the low-pressure ice machine and the condenser outlet of the standard working condition ice machine are connected with the air inlet at the top of the auxiliary liquid storage tank; and a liquid ammonia outlet of the ammonia evaporative condenser is connected with a liquid ammonia inlet on the auxiliary liquid storage tank.
And the ammonia gas discharged from the exhaust port at the top of the ammonia separation tank under the standard working condition passes through the ice maker under the standard working condition and then enters the ammonia gas inlet of the ammonia evaporative condenser together with the ammonia gas exhaust port at the top of the auxiliary liquid storage tank.
Further, ammonia gas discharged from an exhaust port 4401 at the top of the low-pressure ammonia separation tank enters the low-pressure ice maker through an inlet 4402 of the low-pressure ice maker and then enters a heat transfer pipe in the ammonia gas cooler, an outlet of the heat transfer pipe in the cooler is connected with an inlet of a heavy component removal reboiler in the heavy component removal tower, an inlet of a cooling water pipeline in the ammonia gas cooler is connected with a circulating water main pipe, and an outlet of the cooling water pipeline in the cooler is connected with a circulating water return main pipe.
Further, the ammonia blast pipe at liquid storage pot and supplementary liquid storage tank top still is connected with discharge system, particularly, discharge system includes buffer tank V901, tail gas water seal jar V902, collection liquid jar V903, the buffer tank be equipped with high-pressure gas advance pipe 902 and with the ammonia blast pipe at liquid storage pot and supplementary liquid storage tank top is connected, the leakage fluid dram of buffer tank and tail gas water seal tank bottom all with collection liquid jar is connected, the blast pipe at buffer tank top is connected with the air inlet on the tail gas water seal jar.
Further, a liquid discharge port 1903 at the bottom of the carbon dioxide buffer tank and a liquid discharge port 201 at the bottom of the separation tank in front of the carbon dioxide compressor are connected to a liquid collection tank, and a submerged pump P901 is provided in the liquid collection tank to discharge the liquid in the liquid collection tank through a liquid discharge pipe 904 on the submerged pump.
The working principle of the precooling system is as follows:
the system is used for extracting CO from tail gas in the production of carbonic ester2The description is given for the sake of example.
First, the composition of the upstream incoming gas (feed gas) is as follows:
| name (R) | CO2 | Propylene oxide | N2 | CH3OH | Propylene carbonate | Propylene glycol-1, 2 |
| Volume fraction | 88％ | 10％ | 1.94％ | 0.02％ | 0.02％ | 0.02％ |
The temperature is 15 ℃ and 3 KP. The upstream incoming gas firstly enters a carbon dioxide buffer tank V105, the temperature in the carbon dioxide buffer tank V105 is 12 ℃, the upstream incoming gas forms condensate in the buffer tank and is discharged into a liquid collecting tank for post-treatment, and the gas enters a carbon dioxide blower C101 from the buffer tank and is guided to a rear precooler E101 by the carbon dioxide blower.
In the precooler E101, the gas is condensed to-22 ℃ after entering the precooler, the pressure is 5KP at this time, and then enters the front knockout drum V101 of the carbon dioxide compressor.
In the front separation tank V101 of the carbon dioxide compressor, condensate is discharged into a post-treatment system, and CO in the discharged liquid is 0 DEG C2The content of the carbon dioxide is 4.3%, the balance is PO 93.9%, methanol 0.2%, allyl alcohol 0.7%, propylene glycol 0.9% and EO 0.02%, the gas containing more carbon dioxide enters a carbon dioxide compressor C102, and the gas compressed by the carbon dioxide compressor C102 enters a carbon dioxide cooler E102 at the rear end.
The carbon dioxide cooler E102 is a water-cooled cooler, the inlet and the outlet of a heat exchange pipe in the carbon dioxide cooler E102 are respectively connected with a circulating water inlet main pipe and a circulating water return main pipe, and gas treated by the carbon dioxide cooler E102 is discharged and enters CO2In the extraction and refining system, condensate is discharged into a front separation tank of a carbon dioxide compressor, and CO in the condensate is2The content is 37.0 percent, so that the pre-cooling treatment of the tail gas can be completed.
In CO2In the extraction and purification system, CO295.0 percent, 3.4 percent of PO, 21.6 percent of N, 32ppm of methanol, 34ppm of EO, 30 ℃ and 2.5MPa, the mixture is firstly put into a de-heavy tower for primary rectification, heavy components are directly discharged into a precooler after the rectification of the de-heavy tower, the temperature of the discharged heavy components is minus 44 ℃ and 0.5MPa, and the discharged heavy components contain CO275.63%, PO 24.34%, methanol 0.01%, EO 0.02%. The heavy kettle liquid enters a front separation tank of a carbon dioxide compressor after passing through a precooler, the front separation tank of the carbon dioxide compressor discharges separated gas into a carbon dioxide buffer tank, and separated liquid enters a liquid collecting tank in a discharge system.
The light components rectified by the heavy component removing tower enter a heavy component removing condenser for condensation, then enter a heavy component removing separation tank for gas-liquid separation, the condensate separated by the heavy component removing separation tank enters the heavy component removing tower again for rectification, the light components enter the light component removing condenser at the rear end, and the gas separated by the heavy component removing separation tank has the temperature of-11 ℃ and the pressure of 2.49MPa and contains CO298.0％、N22.0％。
Gas separated by the de-heavy separation tankThe light components discharged from the light component removing rectifying tower are condensed in a light component removing condenser, the condensate enters a light component removing separating tank for gas-liquid separation, the separated condensate enters the rectifying tower again for rectification, the separated light component removing gas is discharged to an external system, the temperature of the light component removing gas is-60 ℃, the pressure of the light component removing gas is 5KPa, and the CO content in the light component removing gas is reduced265.0％、 N235.0％。
The heavy still liquid discharged from the light component removing tower is cooled by a cooler to form finished CO product2Finished product of CO2Wherein the temperature is 25 deg.C, 2.1MKPa, and the CO content is2The content is more than 99.995%.
The mass transfer and heat exchange process of the system is as follows:
liquid ammonia is supplemented to enter a liquid storage tank V402 through an inlet 401, the liquid ammonia in the liquid storage tank enters a light-weight removal reboiler, enters an ammonia low-pressure circulating barrel after passing through the light-weight removal reboiler, ammonia in the liquid storage tank enters a light-weight removal reboiler E107, the ammonia after passing through a heavy-weight removal reboiler E106 and a light-weight removal reboiler E107 enters an ammonia low-pressure circulating barrel, the ammonia discharged from the ammonia low-pressure circulating barrel enters an ammonia separating tank under a standard working condition, the ammonia separating tank under the standard working condition is subjected to gas-liquid separation, light gas is discharged into an ice machine under the standard working condition, and then the light gas enters an ammonia evaporative condenser to be condensed and enters an auxiliary liquid storage tank.
The condensed fluid discharged from the standard working condition ammonia separating tank is divided into two paths downwards and respectively enters the heavy component removing condenser and the light component removing condenser to condense the gas entering the heavy component removing condenser and the light component removing condenser, and the ammonia gas discharged from the heavy component removing condenser and the light component removing condenser enters the standard working condition ammonia separating tank again to form circulation.
Meanwhile, the other part of the condenser discharged from the ammonia separating tank under the standard working condition enters a low-pressure ammonia separating tank, condensate discharged from the low-pressure ammonia separating tank enters a subcooler and a second heat transfer pipe in the light component removal condenser for heat exchange and then enters the low-pressure ammonia separating tank again, low-pressure ammonia gas discharged from the low-pressure ammonia separating tank is discharged into a low-pressure ice maker C402, and then enters an ammonia gas cooler for cooling and then enters a reboiler of the heavy component removal tower again.
And the liquid in the auxiliary liquid storage tank enters the condenser in the low-pressure ice machine and then enters the auxiliary liquid storage tank again to form circulation.
Further, in the discharge system in this system, its buffer tank V901 receives the ammonia gas that comes from carbon dioxide compressor front separation tank, liquid storage tank V402 and supplementary liquid storage tank and discharges, and the gas in the buffer tube enters into tail gas water seal tank and adsorbs, and then, tail gas water seal tank and buffer tank exhaust liquid enter into the collection liquid jar, and the submerged pump in the collection liquid jar is handled in discharging its water treatment system in the outer system through leakage fluid dram 904, and the collection liquid jar receives the liquid that comes from carbon dioxide buffer tank discharge simultaneously.
So far, the CO can be completed through the system2Refining extraction, refrigerating heat exchange and discharging.
The embodiments of the present invention are disclosed as the preferred embodiments, but not limited thereto, and those skilled in the art can easily understand the spirit of the present invention and make various extensions and changes without departing from the spirit of the present invention.
Claims (7)
1. CO is contained in carbonic ester production tail gas2Extraction refining system, its characterized in that: comprises a compression precooling system and CO which are connected in series in sequence2An extraction and refining system and a discharge system; wherein, the compression pre-cooling system pre-cools and compresses the feed gas or/and the condensate and then discharges the pre-cooled and compressed feed gas and/or condensate to CO2An extraction and refining system, the CO2The extraction refining system carries out rectification separation on the precooled feed gas or/and condensate to obtain finished product CO2(ii) a By CO2And tail gas and residual liquid discharged after rectification by the extraction and refining system enter the discharge system.
2. A carbonate production off-gas comprising CO according to claim 12Extraction refining system, its characterized in that: the compression precooling system comprises a precooler, a carbon dioxide compressor front separation tank, a carbon dioxide compressor, a carbon dioxide rear cooler, a carbon dioxide rear separation tank and a compressor, wherein the precooler, the carbon dioxide compressor front separation tank, the carbon dioxide compressor, the carbon dioxide rear cooler, the carbon dioxide rear separation tank and the compressor are connected in seriesCarbon dioxide buffer tank, carbon dioxide air-blower, wherein:
the upstream gas enters the carbon dioxide buffer tank, and the carbon dioxide buffer tank enters the precooler after being pressurized by a carbon dioxide blower; the outlet of the precooler is connected with a front separation tank of the carbon dioxide compressor, an exhaust port at the top of the front separation tank of the carbon dioxide compressor is divided into two paths, wherein one path is connected with a discharge system, the other path is connected with an air inlet of the carbon dioxide compressor, and a liquid outlet at the bottom of the front separation tank of the carbon dioxide compressor is a residual liquid discharge port;
the exhaust port of the carbon dioxide compressor is connected with the air inlet of the carbon dioxide aftercooler, the exhaust port at the top of the carbon dioxide aftercooler enters the air inlet of the carbon dioxide afterseparating tank, the condensate discharge port at the bottom of the carbon dioxide afterseparating tank is connected with the front separating tank of the carbon dioxide compressor, and the exhaust port at the top of the carbon dioxide afterseparating tank is connected with the CO2The extraction and refining system is connected, and the gas discharged from the carbon dioxide post-separation tank enters the CO2Rectifying in an extraction and refining system.
3. A carbonate production off-gas comprising CO according to claim 22Extraction refining system, its characterized in that: the CO is2The extraction and refining system comprises a heavy component removing tower, a light component removing tower, a heavy component removing separation tank, a heavy component removing condenser, a light component removing separation tank and a light component removing condenser;
the carbon dioxide enters a heavy component removal tower from an exhaust port at the top of the separation tank for heavy component removal treatment, wherein heavy component kettle liquid enters a precooler through a liquid discharge pipe at the bottom, light components enter a heavy component removal condenser through an exhaust pipe for condensation and then enter the heavy component removal separation tank, and a liquid discharge port at the bottom of the heavy component removal separation tank is connected with an inlet at the top of the heavy component removal tower;
the light components treated by the heavy component removal separation tank and the light components rectified by the light component removal tower enter a light component removal condenser through an exhaust port at the top of the light component removal tower to be condensed and then enter the light component removal separation tank together, the condensed liquid treated by the light component removal separation tank enters the light component removal tower again through a liquid discharge pipe to be rectified, the heavy component kettle liquid rectified by the light component removal tower is condensed by a coolerAfter being CO2Putting the finished product into a storage tank;
the light component gas treated by the light component removing and separating tank is discharged from an exhaust port at the top of the light component removing and separating tank and enters an inlet of a first heat exchange tube in the precooler, and an outlet of the first heat exchange tube in the precooler is emptied;
and a liquid discharge port at the bottom of the de-weighting tower is connected with an inlet of a second heat transfer pipe in the precooler, an outlet of the second heat transfer pipe is connected with the front separation tank of the carbon dioxide compressor, a liquid discharge port at the bottom of the front separation tank of the carbon dioxide compressor is connected with a discharge system, and an air exhaust port at the top of the front separation tank of the carbon dioxide compressor is connected with a carbon dioxide buffer tank.
4. A carbonate production off-gas comprising CO according to claim 32Extraction refining system, its characterized in that: the heavy component removal reboiler in the bottom of the heavy component removal tower and the light component removal reboiler in the bottom of the light component removal tower are connected with ammonia gas or/and liquid ammonia in a refrigeration system, and the outlets of the heavy component removal reboiler and the light component removal reboiler are connected with an ammonia low-pressure circulating barrel;
the system also comprises a standard working condition ammonia separating tank, wherein an exhaust port at the top of the ammonia low-pressure circulating barrel is connected with an inlet of the standard working condition ammonia separating tank, an exhaust port at the top of the standard working condition ammonia separating tank is an ammonia gas exhaust port and enters a refrigeration system, a condensate outlet at the bottom of the standard working condition ammonia separating tank is connected with a heat exchange medium pipe inlet of the de-heavy condenser and a first heat exchange medium inlet of the de-light condenser, and a heat exchange medium pipe outlet of the de-heavy condenser and a first heat exchange medium outlet of the de-light condenser are connected with an inlet of the standard working condition ammonia separating tank;
the system is characterized by further comprising a low-pressure ammonia separation tank, a condensate discharge port at the bottom of the standard working condition ammonia separation tank is further connected with an inlet of the low-pressure ammonia separation tank, an exhaust port at the top of the low-pressure ammonia separation tank is an ammonia gas discharge port and enters a refrigeration system, a condensate outlet at the bottom of the low-pressure ammonia separation tank is connected with a second heat exchange medium inlet of the lightness-removing condenser and a heat exchange medium inlet of the subcooler, and a second heat exchange medium outlet of the lightness-removing condenser and a heat exchange medium outlet of the subcooler are connected with an inlet of the low-pressure ammonia separation tank.
5. A carbonate production off-gas comprising CO according to claim 42Extraction refining system, its characterized in that: further comprises a compression pre-cooling system and a CO2Extract the refrigerating system that refined system, discharge system provided the energy, refrigerating system includes liquid storage pot, supplementary liquid storage pot, ammonia cooler, low pressure ice maker, standard operating mode ice maker, ammonia evaporative condenser, wherein:
the liquid storage tank is connected with the auxiliary liquid storage tank through a pipeline 4012, and liquid ammonia in the auxiliary liquid storage tank can enter the liquid storage tank; ammonia gas exhaust pipes are arranged at the tops of the liquid storage tank and the auxiliary liquid storage tank and are connected with an inlet of a lightness-removing reboiler in the lightness-removing tower, ammonia gas enters the lightness-removing reboiler through the ammonia gas exhaust pipes, and a liquid ammonia discharge pipe is arranged on the liquid storage tank and is connected with an inlet of the lightness-removing reboiler in the lightness-removing tower;
a liquid ammonia liquid discharge pipe at the bottom of the auxiliary liquid storage tank is divided into two paths, wherein one path is connected with the inlet of a condenser of the low-pressure ice machine, and the other path is connected with the inlet of the condenser of the standard working condition ice machine; the condenser outlet of the low-pressure ice machine and the condenser outlet of the standard working condition ice machine are connected with the air inlet at the top of the auxiliary liquid storage tank; a liquid ammonia outlet of the ammonia evaporative condenser is connected with a liquid ammonia inlet on the auxiliary liquid storage tank;
the ammonia gas discharged from the exhaust port at the top of the ammonia separation tank under the standard working condition passes through the ice maker under the standard working condition and then enters the ammonia gas inlet of the ammonia evaporative condenser together with the ammonia gas exhaust port at the top of the auxiliary liquid storage tank;
the ammonia gas discharged from an exhaust port at the top of the low-pressure ammonia separation tank enters a heat transfer pipe in an ammonia gas cooler after passing through a low-pressure ice maker, the outlet of the heat transfer pipe in the cooler is connected with the inlet of a heavy component removal reboiler in a heavy component removal tower, the inlet of a cooling water pipeline in the ammonia gas cooler is connected with a circulating water main pipe, and the outlet of the cooling water pipeline in the cooler is connected with a circulating water return main pipe;
and the ammonia gas exhaust pipes at the tops of the liquid storage tank and the auxiliary liquid storage tank are also connected with a discharge system.
6. A carbonate production off-gas according to claim 5 comprising CO2Extraction refining system, its characterized in that: the discharge system comprises a buffer tank, a tail gas water seal tank and a liquid collecting tank, wherein the buffer tank is provided with a high-pressure gas inlet pipe and is connected with the liquid storage tank and an ammonia gas exhaust pipe at the top of the auxiliary liquid storage tank, liquid discharge ports at the bottoms of the buffer tank and the tail gas water seal tank are connected with the liquid collecting tank, and the exhaust pipe at the top of the buffer tank is connected with a gas inlet on the tail gas water seal tank.
7. A carbonate production off-gas according to claim 5 comprising CO2Extraction refining system, its characterized in that: and the liquid outlet at the bottom of the carbon dioxide buffer tank and the liquid outlet at the bottom of the front separation tank of the carbon dioxide compressor are connected with the liquid collection tank, and the liquid collection tank is internally provided with a submerged pump and discharges the liquid in the liquid collection tank.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202020751692.4U CN212680522U (en) | 2020-05-08 | 2020-05-08 | CO 2-containing extraction and refining system in carbonate production tail gas |
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| CN202020751692.4U CN212680522U (en) | 2020-05-08 | 2020-05-08 | CO 2-containing extraction and refining system in carbonate production tail gas |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111675220A (en) * | 2020-05-08 | 2020-09-18 | 江西江氨科技有限公司 | CO is contained in tail gas generated in carbonate production2Extraction and refining system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111675220A (en) * | 2020-05-08 | 2020-09-18 | 江西江氨科技有限公司 | CO is contained in tail gas generated in carbonate production2Extraction and refining system |
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