CN111675220B - CO-containing in tail gas from carbonate production 2 Extraction and refining system - Google Patents
CO-containing in tail gas from carbonate production 2 Extraction and refining system Download PDFInfo
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- CN111675220B CN111675220B CN202010390302.XA CN202010390302A CN111675220B CN 111675220 B CN111675220 B CN 111675220B CN 202010390302 A CN202010390302 A CN 202010390302A CN 111675220 B CN111675220 B CN 111675220B
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Abstract
The invention provides a method for treating CO in tail gas 2 CO contained in the tail gas of the carbonate production for extraction 2 The extraction and refining system comprises a compression pre-cooling system and a CO which are sequentially connected in series 2 An extraction and refining system and an emission system; wherein, the compression pre-cooling system pre-cooling and compressing the feed gas or/and condensate, and then discharging the feed gas or/and condensate into CO 2 An extraction and purification system for CO 2 The extraction refining system rectifies and separates the precooled raw material gas or/and condensate to obtain a finished product CO 2 The method comprises the steps of carrying out a first treatment on the surface of the Through CO 2 And (3) introducing tail gas and residual liquid discharged after rectification of the extraction and refining system into the discharge 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 in tail gas produced in carbonate production 2 An extraction and refining system.
Background
In the carbonate preparation system, the tail gas generated in the production of the carbonate contains a large amount of CO 2 Equal-high pollution and toxic gas, and CO in tail gas 2 And the like are common industrial raw materials, and thus, for example, CO in tail gas thereof 2 The extraction treatment can reduce the problem of exhaust emission pollution, and bring economic benefit to production enterprises, so the design provides a CO-containing device 2 CO of industrial tail gas 2 And (5) refining the extraction system.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and adapt to the actual needs, and provides a catalyst containing CO in the tail gas of carbonate production 2 An extraction and refining system.
In order to achieve the purpose of the invention, the technical scheme adopted by the invention is as follows:
discloses a method for preparing carbonic ester tail gas containing CO 2 The extraction and refining system comprises a compression pre-cooling system and a CO which are sequentially connected in series 2 An extraction and refining system and an emission system; wherein, the compression pre-cooling system pre-cooling and compressing the feed gas or/and condensate, and then discharging the feed gas or/and condensate into CO 2 An extraction and purification system for CO 2 The extraction refining system rectifies and separates the precooled raw material gas or/and condensate to obtain a finished product CO 2 The method comprises the steps of carrying out a first treatment on the surface of the Through CO 2 And (3) introducing tail gas and residual liquid discharged after rectification of the extraction and refining system into the discharge system.
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, a carbon dioxide buffer tank and a carbon dioxide blower which are connected in series, wherein:
upstream incoming gas enters the carbon dioxide buffer tank, and the carbon dioxide buffer tank enters the precooler after being pressurized by the carbon dioxide blower; the outlet of the precooler is connected with a 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 an exhaust 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 exhaust port;
the exhaust port of the carbon dioxide compressor is connected with the air inlet of the carbon dioxide aftercooler, the top exhaust port of the carbon dioxide aftercooler enters the air inlet of the carbon dioxide afterseparating tank, the condensate exhaust port at the bottom of the carbon dioxide afterseparating tank is connected with the carbon dioxide separating tank, and the exhaust port at the top of the carbon dioxide afterseparating tank is connected with CO 2 The extraction and refining system is connected, and the gas discharged from the separation tank after carbon dioxide enters the CO 2 Rectifying in an extraction and refining system.
The CO 2 The extraction refining system comprises a heavy removal tower, a light removal tower, a heavy removal separating tank, a heavy removal condenser, a light removal separating tank and a light removal condenser;
the method comprises the steps that an exhaust port at the top of a carbon dioxide rear separation tank enters a heavy-removal tower for heavy-removal treatment, wherein heavy component kettle liquid enters a precooler through a liquid discharge pipe at the bottom, light components enter a heavy-removal condenser through an exhaust pipe for condensation and then enter the heavy-removal separation tank, and a liquid discharge port at the bottom of the heavy-removal separation tank is connected with an inlet at the top of the heavy-removal tower;
the light component treated by the heavy removal separation tank enters the light removal separation tank; meanwhile, the light components after rectification of 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 a light component removal separation tank, condensate treated by the light component removal separation tank enters the light component removal tower again through a liquid discharge pipe to be rectified, and heavy component kettle liquid after rectification of the light component removal tower is condensed by a condenser to be CO 2 Finished productEntering into the storage tank;
the light component gas treated by the light component removal separation tank is discharged through an exhaust port at the top of the light component removal separation 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;
the liquid outlet at the bottom of the de-weight tower is connected with the inlet of a second heat transfer tube in the precooler, the outlet of the second heat transfer tube is connected with the carbon dioxide separation tank, the liquid outlet at the bottom of the carbon dioxide separation tank is connected with the discharge system, and the air outlet at the top of the carbon dioxide separation tank is connected with the carbon dioxide buffer tank.
The heavy removal reboiler in the bottom of the heavy removal tower and the light removal reboiler inlet in the bottom of the light removal tower are connected with ammonia gas or/and liquid ammonia in a refrigerating system, and the outlets of the heavy removal reboiler and the light removal reboiler are connected with an ammonia low-pressure circulation barrel;
the system comprises a standard working condition ammonia separation tank, wherein an exhaust port at the top of an ammonia low-pressure circulation barrel is connected with an inlet of the standard working condition ammonia separation tank, an exhaust port at the top of the standard working condition ammonia separation tank is an ammonia exhaust port and enters a refrigerating system, a condensate outlet at the bottom of the standard working condition ammonia separation tank is connected with a heat exchange medium pipe inlet of a heavy removal condenser and a first heat exchange medium inlet of a light removal condenser, and a heat exchange medium pipe outlet of the heavy removal condenser and a first heat exchange medium outlet of the light removal condenser are connected with an inlet of the standard working condition ammonia separation tank;
the low-pressure ammonia separation device comprises a low-pressure ammonia separation tank, wherein a condensate outlet at the bottom of the low-pressure ammonia separation tank is connected with an inlet of the low-pressure ammonia separation tank, an exhaust outlet at the top of the low-pressure ammonia separation tank is an ammonia outlet and enters a refrigerating system, a condensate outlet at the bottom of the low-pressure ammonia separation tank is connected with a second heat exchange medium inlet of a light-removal condenser and a heat exchange medium inlet of a subcooler, and a second heat exchange medium outlet of the light-removal condenser and a heat exchange medium outlet of the subcooler are connected with an inlet of the low-pressure ammonia separation tank.
Also comprises a pre-cooling system and CO for the compression 2 Refrigerating system for providing energy source by extracting and refining system and discharging system, the refrigerating system comprises a liquid storage tank and an auxiliary liquid storage tankTank, ammonia cooler, low pressure ice machine, standard operating mode ice machine, ammonia evaporation 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; the top of the liquid storage tank and the auxiliary liquid storage tank are provided with an ammonia gas exhaust pipe and are connected with an inlet of a light-removal reboiler in the light-removal tower, ammonia gas enters the light-removal reboiler through the ammonia gas exhaust pipe, and the liquid storage tank is provided with a liquid ammonia exhaust pipe and is connected with an inlet of the light-removal reboiler in the light-removal tower;
the 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 condenser inlet of the low-pressure ice machine, and the other path is connected with the condenser inlet 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; the liquid ammonia outlet of the ammonia evaporation condenser is connected with a liquid ammonia inlet on the auxiliary liquid storage tank;
ammonia gas discharged from an exhaust port at the top of the standard working condition ammonia separation tank passes through the standard working condition ice machine and then enters an ammonia gas inlet of the ammonia evaporation condenser together with an ammonia gas outlet at the top of the auxiliary liquid storage tank;
ammonia gas discharged from an exhaust port at the top of the low-pressure ammonia separation tank enters a heat transfer pipe in the ammonia gas cooler after passing through a low-pressure ice maker, an outlet of the heat transfer pipe in the cooler is connected with an inlet of a weight-removing reboiler in the weight-removing tower, a cooling water pipeline inlet in the ammonia gas cooler is connected with a circulating water main pipe, and a cooling water pipeline outlet in the cooler is connected with a circulating water return main pipe;
the ammonia gas exhaust pipe at the top of the liquid storage tank and the auxiliary liquid storage tank is also connected with an exhaust system.
The exhaust 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 an ammonia gas exhaust pipe at the top of the liquid storage tank and an auxiliary liquid storage tank, liquid draining 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 an air inlet on the tail gas water seal tank.
The liquid outlet at the bottom of the carbon dioxide buffer tank and the liquid outlet at the bottom of the carbon dioxide separation tank are connected with the liquid collecting tank, and a submerged pump is arranged in the liquid collecting tank and discharges liquid in the liquid collecting tank.
The invention has the beneficial effects that:
CO-containing of the design 2 CO of industrial tail gas 2 The refining extraction system has simple structure and easy realization, and can treat CO in the tail gas treatment system 2 The extraction is carried out, the problem of direct exhaust pollution is solved, and meanwhile, the economic benefit of enterprises can be improved.
Drawings
Fig. 1 is a schematic diagram of the principle of the compression pre-cooling system of the present invention;
FIG. 2 is a graph of CO in the present invention 2 Schematic diagram of main principle of extraction and refining system;
FIG. 3 is a schematic diagram of the main principle of the refrigeration system according to the present invention;
fig. 4 is a schematic diagram of the main principle of the exhaust system in the present invention.
Detailed Description
The invention is further illustrated by the following examples in conjunction with the accompanying drawings:
example 1: CO contained in tail gas from carbonate production 2 Extraction and refinement systems, see fig. 1-4.
Comprises a compression precooling system and CO which are connected in series in turn 2 An extraction and refining system and an emission system; the principle is that the compression pre-cooling system pre-cools and compresses the feed gas or/and condensate liquid and then discharges the feed gas or/and condensate liquid into CO 2 An extraction and purification system for CO 2 The extraction refining system rectifies and separates the precooled raw material gas or/and condensate to obtain a finished product CO 2 The method comprises the steps of carrying out a first treatment on the surface of the Through CO 2 And (3) introducing tail gas and residual liquid discharged after rectification of the extraction and refining system into the discharge system.
Specifically, the compression pre-cooling system includes a pre-cooler E101, a carbon dioxide pre-compressor separation tank V101, a carbon dioxide compressor C102, a carbon dioxide post-cooler E102, a carbon dioxide post-separation tank V102, a carbon dioxide buffer tank V105, and a carbon dioxide blower C101 connected in series, wherein:
upstream incoming gas enters the carbon dioxide buffer tank, and the carbon dioxide buffer tank enters the precooler after being pressurized by the carbon dioxide blower; the outlet of the precooler is connected with the front separating tank of the carbon dioxide compressor, the exhaust port at the top of the front separating tank of the carbon dioxide compressor is divided into two paths, one path is connected with the exhaust 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 separating tank of the carbon dioxide compressor is a residual night exhaust port.
Further, the exhaust port of the carbon dioxide compressor is connected with the air inlet of the carbon dioxide aftercooler, the top exhaust port of the carbon dioxide aftercooler enters the air inlet of the carbon dioxide afterseparating tank, the condensate exhaust port at the bottom of the carbon dioxide afterseparating tank is connected with the carbon dioxide separating tank V201, and the exhaust port at the top of the carbon dioxide afterseparating tank is connected with CO 2 The extraction and refining system is connected, and the gas discharged from the separation tank after carbon dioxide enters the CO 2 Rectifying in an extraction and refining system.
In particular, the CO 2 The extraction refining system comprises a heavy-removal tower T101, a light-removal tower T102, a heavy-removal separation tank V103, a heavy-removal condenser E103, a light-removal separation tank V104 and a light-removal condenser E104; wherein, the exhaust port 1101 at the top of the separation tank after carbon dioxide enters the de-weight tower for de-weight treatment, wherein, heavy component kettle liquid enters the precooler through the liquid discharge pipe 1102 at the bottom, light component enters the de-weight separation tank after entering the de-weight condenser through the exhaust pipe for condensation, and the liquid discharge port at the bottom of the de-weight separation tank is connected with the inlet at the top of the de-weight tower to form circulation.
Further, the light component treated by the heavy removal separation tank enters the light removal separation tank; meanwhile, the light components rectified by the light component removing tower enter a light component removing condenser through an exhaust port at the top of the light component removing tower to be condensed, and then enter a light component removing separating tank, the condensate processed by the light component removing separating tank enters the light component removing tower again through a liquid discharge pipe to be rectified to form circulation, and the heavy component kettle liquid rectified by the light component removing tower is condensed by a condenser to be CO 2 And the finished product enters a storage tank.
Further, the light component gas treated by the light component removal separation tank is discharged from the exhaust port 1103 at the top of the light component removal separation tank and enters the inlet of the first heat exchange tube in the precooler, and the outlet of the first heat exchange tube in the precooler is emptied.
Further, the liquid discharge pipe 1102 at the bottom of the de-weight tower is connected with the inlet of a second heat transfer pipe in the precooler, the outlet of the second heat transfer pipe is connected with the carbon dioxide separation tank V201, the liquid discharge port 201 at the bottom of the carbon dioxide separation tank is connected with a discharge system, and the air outlet at the top of the carbon dioxide separation tank V201 is connected with a carbon dioxide buffer tank.
Further, in the system, the inlets of the heavy removal reboiler E106 in the bottom of the heavy removal tower and the light removal reboiler E107 in the bottom of the light removal tower are connected with ammonia gas or/and liquid ammonia in a refrigerating system, and the outlets of the heavy removal reboiler E106 and the light removal reboiler E107 are connected with an ammonia low-pressure circulation barrel V403.
Further, the system also comprises a standard working condition ammonia separation tank V404A, an exhaust port at the top of the ammonia low-pressure circulation barrel is connected with an inlet of the standard working condition ammonia separation tank V404A, an exhaust port at the top of the standard working condition ammonia separation tank V404A is an ammonia exhaust port 4401 and enters the refrigeration system, a condensate outlet at the bottom of the standard working condition ammonia separation tank is connected with a heat exchange medium pipe inlet of the heavy removal condenser and a first heat exchange medium inlet of the light removal condenser, and a heat exchange medium pipe outlet of the heavy removal condenser and a first heat exchange medium outlet of the light removal condenser are connected with an inlet of the standard working condition ammonia separation tank.
The low-pressure ammonia separation device is characterized by further comprising a low-pressure ammonia separation tank V405, wherein a condensate outlet at the bottom of the standard working condition ammonia separation tank is connected with an inlet of the low-pressure ammonia separation tank, an exhaust port 4402 at the top of the low-pressure ammonia separation tank is an ammonia outlet and enters a refrigerating 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 light removal condenser and a heat exchange medium inlet of the subcooler, and a second heat exchange medium outlet of the light removal condenser and a heat exchange medium outlet of the subcooler are connected with an inlet of the low-pressure ammonia separation tank.
Further, the system also comprises a compression precooling system and CO 2 The refrigeration system for providing energy by the extraction refining system and the discharge system comprises a liquid storage tank V402, an auxiliary liquid storage tank V401, an ammonia cooler E402, a low-pressure ice machine C402, a standard working condition ice machine C401 and an ammonia evaporation 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 are provided with an ammonia gas exhaust pipe 4102 and are connected with an inlet of a light-removal reboiler in the light-removal tower, ammonia gas enters the light-removal reboiler through the ammonia gas exhaust pipe, and the liquid storage tank is provided with a liquid ammonia exhaust pipe 4101 and is connected with an inlet of the light-removal reboiler in the light-removal tower.
The 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 condenser inlet of the low-pressure ice machine, and the other path is connected with the condenser inlet 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 evaporation condenser is connected with a liquid ammonia inlet on the auxiliary liquid storage tank.
And ammonia gas discharged from an exhaust port at the top of the standard working condition ammonia separation tank passes through the standard working condition ice machine and then enters the ammonia gas inlet of the ammonia evaporation condenser together with an ammonia gas outlet at the top of the auxiliary liquid storage tank.
Further, ammonia gas discharged from an ammonia gas outlet 4402 at the top of the low-pressure ammonia separation tank enters the heat transfer pipe in the ammonia gas cooler after entering the low-pressure ice machine through the inlet of the low-pressure ice machine, the outlet of the heat transfer pipe in the cooler is connected with the inlet of the heavy removal reboiler in the heavy removal tower, the inlet of the cooling water pipeline in the ammonia gas cooler is connected with the circulating water main pipe, and the outlet of the cooling water pipeline in the cooler is connected with the circulating water return main pipe.
Further, the ammonia gas exhaust pipe at the top of the liquid storage tank and the auxiliary liquid storage tank is also connected with an exhaust system, specifically, the exhaust system comprises a buffer tank V901, a tail gas water seal tank V902 and a liquid collection tank V903, the buffer tank is provided with a high-pressure gas inlet pipe 902 and is connected with the ammonia gas exhaust pipe at the top of the liquid storage tank and the auxiliary liquid storage tank, liquid outlets at the bottom of the buffer tank and the tail gas water seal tank are connected with the liquid collection tank, and the exhaust pipe at the top of the buffer tank is connected with an air inlet on the tail gas water seal tank.
Further, the liquid outlet 1903 at the bottom of the carbon dioxide buffer tank and the liquid outlet 201 at the bottom of the carbon dioxide separation tank are connected to a liquid collecting tank, and a submerged pump P901 is provided in the liquid collecting tank and the liquid in the liquid collecting tank is discharged through a liquid outlet pipe 904 on the submerged pump.
The working principle of the precooling system of the design is as follows:
the system extracts CO from tail gas in the production of carbonic ester 2 An example is described.
First, the upstream incoming gas (feed gas) is composed of the following components:
the temperature was 15℃and 3KP. The upstream gas enters the carbon dioxide buffer tank V105, the temperature in the carbon dioxide buffer tank V105 is 12 ℃, condensate formed in the buffer tank by the upstream gas is discharged into the liquid collection tank for post-treatment, and the gas enters the carbon dioxide blower C101 from the buffer tank and is guided to the precooler E101 at the rear by the carbon dioxide blower.
In the precooler E101, the gas enters the precooler and is condensed to-22 ℃ at a pressure of 5KP, and then enters the separation tank V101 before the carbon dioxide compressor.
In the separation tank V101 before the carbon dioxide compressor, the condensate is discharged into the post-treatment system, at the moment, the discharged liquid is at 0 ℃ and CO is discharged 2 4.3% of PO93.9%, 0.2% of methanol, 0.7% of allyl alcohol, 0.9% of propylene glycol and 0.02% of EO, and the gas containing more carbon dioxide enters a carbon dioxide compressor C102, and the gas after being compressed by the carbon dioxide compressor C102 enters a carbon dioxide aftercooler E102 at the rear end.
The carbon dioxide aftercooler E102 is a water-cooled cooler, the inlet and the outlet of a heat exchange pipe in the carbon dioxide aftercooler E102 are respectively connected with a circulating water inlet main pipe and a circulating water return main pipe, and the gas treated by the carbon dioxide aftercooler E102 is discharged and enters CO 2 In the extraction refining system, condensate liquid is discharged into a carbon dioxide separation tank, and CO in the condensate liquid 2 The content is 37.0%, so that the precooling treatment of the tail gas can be finished.
In CO 2 In the extraction and refining system, CO 2 95.0 percent, PO3.4 percent, N21.6 percent, 32ppm of methanol, 34ppm of EO, and the temperature of 30 ℃ and 2.5MPa, firstly enters a de-weight tower for primary rectification, the heavy components of the de-weight tower after rectification are directly discharged into a precooler, the temperature of the discharged heavy components is-44 ℃ and 0.5MPa, and the CO is contained in the discharged heavy components 2 75.63%, PO24.34%, methanol 0.01%, EO0.02%. The heavy kettle liquid enters a carbon dioxide separation tank after passing through a precooler, the carbon dioxide separation tank discharges the separated gas into a carbon dioxide buffer tank, and the separated liquid enters a liquid collecting tank in a discharge system.
Condensing the light component after rectification in a heavy removal tower in a heavy removal condenser, then separating gas and liquid in a heavy removal separating tank, re-rectifying the condensate separated in the heavy removal separating tank in the heavy removal tower, and separating the light component in the light removal condenser at the rear end at-11 ℃ and 2.49MPa in the gas containing CO 2 98.0%、N 2 2.0%。
The gas separated by the weight-removing separation tank enters a weight-removing condenser along with the light components discharged by the weight-removing rectification column to be condensed, then the condensate enters the weight-removing separation tank to be subjected to gas-liquid separation, the separated condensate enters the rectification column again to be rectified, the separated weight-removing gas is discharged into an external system, the temperature of the weight-removing gas is-60 ℃, 5KPa and CO content is contained 2 65.0%、N 2 35.0%。
Heavy kettle liquid discharged from the light component removing tower passes through a cooler to form finished CO 2 Finished CO 2 Wherein the temperature is 25 ℃, 2.1MKPa, and the CO is 2 The content is more than 99.995 percent.
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, liquid ammonia in the liquid storage tank enters a light removal reboiler, enters an ammonia low-pressure circulation barrel after passing through the light removal reboiler, ammonia in the liquid storage tank enters a light removal reboiler E107, ammonia after passing through a heavy removal reboiler E106 and the light removal reboiler E107 enters the ammonia low-pressure circulation barrel, ammonia discharged through the ammonia low-pressure circulation barrel enters a standard working condition ammonia separation tank, the standard working condition ammonia separation tank performs gas-liquid separation, light gas of the liquid ammonia is discharged into a standard working condition ice machine, and then enters an auxiliary liquid storage tank after entering an ammonia evaporation condenser for condensation.
The condensate discharged from the standard working condition ammonia separation tank is downwards divided into two paths which respectively enter the heavy-removal condenser and the light-removal condenser to condense the gas entering the heavy-removal condenser and the light-removal condenser, and the ammonia discharged from the heavy-removal condenser and the light-removal condenser enters the standard working condition ammonia separation tank again to form circulation.
Meanwhile, the other part of the condenser discharged from the ammonia separation tank under the standard working condition enters the low-pressure ammonia separation tank, condensate discharged from the low-pressure ammonia separation tank enters the subcooler and the second heat transfer pipe in the light-removal condenser for heat exchange and then enters the low-pressure ammonia separation tank again, low-pressure ammonia discharged from the low-pressure ammonia separation tank enters the low-pressure ice machine C402, and then enters the ammonia cooler for cooling and then enters the heavy-removal tower reboiler 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 exhaust system in this system, its buffer tank V901 receives the ammonia gas from the separation tank, the liquid storage tank V402 and the auxiliary liquid storage tank before the carbon dioxide compressor, and the gas in the buffer tube enters into the tail gas water seal tank to be adsorbed, then, the liquid in the tail gas water seal tank and the buffer tank enters into the liquid collection tank, the submerged pump in the liquid collection tank discharges it into the water treatment system in the external system for treatment through the liquid discharge pipe 904, and the liquid collection tank simultaneously receives the liquid from the carbon dioxide buffer tank.
So far, the CO can be completed through the system 2 Refining extraction, refrigerating heat exchange and discharge.
The embodiments of the present invention are disclosed as preferred embodiments, but not limited thereto, and those skilled in the art will readily appreciate from the foregoing description that various extensions and modifications can be made without departing from the spirit of the present invention.
Claims (5)
1. CO contained in tail gas from carbonate production 2 The extraction and refining system is characterized in that: comprises a compression precooling system and CO which are connected in series in turn 2 An extraction and refining system and an emission system; wherein, the compression pre-cooling system pre-cooling and compressing the feed gas or/and condensate, and then discharging the feed gas or/and condensate into CO 2 An extraction and purification system for CO 2 The extraction refining system rectifies and separates the precooled raw material gas or/and condensate to obtain a finished product CO 2 The method comprises the steps of carrying out a first treatment on the surface of the Through CO 2 Tail gas and residual liquid discharged after rectification of the extraction and refining system enter the discharge system;
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, a carbon dioxide buffer tank and a carbon dioxide blower which are connected in series, wherein:
upstream incoming gas enters the carbon dioxide buffer tank, and the carbon dioxide buffer tank enters the precooler after being pressurized by the carbon dioxide blower; the outlet of the precooler is connected with a 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 an exhaust 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 exhaust port;
the exhaust port of the carbon dioxide compressor is connected with the air inlet of the carbon dioxide aftercooler, the top exhaust port of the carbon dioxide aftercooler enters the air inlet of the carbon dioxide afterseparating tank, the condensate exhaust 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 CO 2 The extraction and refining system is connected, and the gas discharged from the separating tank after carbon dioxide entersInto the CO 2 Rectifying in an extraction refining system;
the CO 2 The extraction refining system comprises a heavy removal tower, a light removal tower, a heavy removal separating tank, a heavy removal condenser, a light removal separating tank and a light removal condenser;
the method comprises the steps that an exhaust port at the top of a carbon dioxide rear separation tank enters a heavy-removal tower for heavy-removal treatment, wherein heavy component kettle liquid enters a precooler through a liquid discharge pipe at the bottom, light components enter a heavy-removal condenser through an exhaust pipe for condensation and then enter the heavy-removal separation tank, and a liquid discharge port at the bottom of the heavy-removal separation tank is connected with an inlet at the top of the heavy-removal tower;
the light component treated by the heavy removal separation tank enters the light removal separation tank; meanwhile, the light components after rectification of 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 a light component removal separation tank, condensate treated by the light component removal separation tank enters the light component removal tower again through a liquid discharge pipe to be rectified, and heavy component kettle liquid after rectification of the light component removal tower is condensed by a condenser to be CO 2 The finished product enters a storage tank;
the light component gas treated by the light component removal separation tank is discharged through an exhaust port at the top of the light component removal separation 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;
the liquid outlet at the bottom of the de-weight tower is connected with the inlet of a second heat transfer tube in the precooler, the outlet of the second heat transfer tube is connected with a carbon dioxide separation tank, the liquid outlet at the bottom of the carbon dioxide separation tank is connected with a discharge system, and the air outlet at the top of the carbon dioxide separation tank is connected with a carbon dioxide buffer tank.
2. The CO-containing tail gas from the production of carbonates according to claim 1 2 The extraction and refining system is characterized in that: the heavy removal reboiler in the bottom of the heavy removal tower and the light removal reboiler inlet in the bottom of the light removal tower are connected with ammonia gas or/and liquid ammonia in a refrigerating system, and the outlets of the heavy removal reboiler and the light removal reboiler are connected with an ammonia low-pressure circulation barrel;
the system comprises a standard working condition ammonia separation tank, wherein an exhaust port at the top of an ammonia low-pressure circulation barrel is connected with an inlet of the standard working condition ammonia separation tank, an exhaust port at the top of the standard working condition ammonia separation tank is an ammonia exhaust port and enters a refrigerating system, a condensate outlet at the bottom of the standard working condition ammonia separation tank is connected with a heat exchange medium pipe inlet of a heavy removal condenser and a first heat exchange medium inlet of a light removal condenser, and a heat exchange medium pipe outlet of the heavy removal condenser and a first heat exchange medium outlet of the light removal condenser are connected with an inlet of the standard working condition ammonia separation tank;
the low-pressure ammonia separation device comprises a low-pressure ammonia separation tank, wherein a condensate outlet at the bottom of the low-pressure ammonia separation tank is connected with an inlet of the low-pressure ammonia separation tank, an exhaust outlet at the top of the low-pressure ammonia separation tank is an ammonia outlet and enters a refrigerating system, a condensate outlet at the bottom of the low-pressure ammonia separation tank is connected with a second heat exchange medium inlet of a light-removal condenser and a heat exchange medium inlet of a subcooler, and a second heat exchange medium outlet of the light-removal condenser and a heat exchange medium outlet of the subcooler are connected with an inlet of the low-pressure ammonia separation tank.
3. The CO-containing tail gas from the production of carbonates according to claim 2 2 The extraction and refining system is characterized in that: also comprises a pre-cooling system and CO for the compression 2 The refrigerating system for providing energy by the extraction refining system and the discharge system comprises a liquid storage tank, an auxiliary liquid storage tank, an ammonia cooler, a low-pressure ice machine, a standard working condition ice machine and an ammonia evaporation 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; the top of the liquid storage tank and the auxiliary liquid storage tank are provided with an ammonia gas exhaust pipe and are connected with an inlet of a light-removal reboiler in the light-removal tower, ammonia gas enters the light-removal reboiler through the ammonia gas exhaust pipe, and the liquid storage tank is provided with a liquid ammonia exhaust pipe and is connected with an inlet of the light-removal reboiler in the light-removal tower;
the 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 condenser inlet of the low-pressure ice machine, and the other path is connected with the condenser inlet 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; the liquid ammonia outlet of the ammonia evaporation condenser is connected with a liquid ammonia inlet on the auxiliary liquid storage tank;
ammonia gas discharged from an exhaust port at the top of the standard working condition ammonia separation tank passes through the standard working condition ice machine and then enters an ammonia gas inlet of the ammonia evaporation condenser together with an ammonia gas outlet at the top of the auxiliary liquid storage tank;
ammonia gas discharged from an exhaust port at the top of the low-pressure ammonia separation tank enters a heat transfer pipe in the ammonia gas cooler after passing through a low-pressure ice maker, an outlet of the heat transfer pipe in the cooler is connected with an inlet of a weight-removing reboiler in the weight-removing tower, a cooling water pipeline inlet in the ammonia gas cooler is connected with a circulating water main pipe, and a cooling water pipeline outlet in the cooler is connected with a circulating water return main pipe;
the ammonia gas exhaust pipe at the top of the liquid storage tank and the auxiliary liquid storage tank is also connected with an exhaust system.
4. A CO-containing tail gas from the production of carbonates according to claim 3 2 The extraction and refining system is characterized in that: the exhaust 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 an ammonia gas exhaust pipe at the top of the liquid storage tank and an auxiliary liquid storage tank, liquid draining 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 an air inlet on the tail gas water seal tank.
5. A CO-containing tail gas from the production of carbonates according to claim 3 2 The extraction and refining system is characterized in that: the liquid outlet at the bottom of the carbon dioxide buffer tank and the liquid outlet at the bottom of the carbon dioxide separation tank are connected with the liquid collecting tank, and a submerged pump is arranged in the liquid collecting tank and discharges liquid in the liquid collecting tank.
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| CN113149011A (en) * | 2021-03-23 | 2021-07-23 | 江西江氨科技有限公司 | Method and system for recovering alcohol and high-purity carbon dioxide by using alcohol tail gas as raw material |
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