CN212893938U - Containing CO2CO of industrial tail gas2Refining and extracting system - Google Patents
Containing CO2CO of industrial tail gas2Refining and extracting system Download PDFInfo
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- CN212893938U CN212893938U CN202020751685.4U CN202020751685U CN212893938U CN 212893938 U CN212893938 U CN 212893938U CN 202020751685 U CN202020751685 U CN 202020751685U CN 212893938 U CN212893938 U CN 212893938U
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Abstract
The utility model provides a CO in tail gas2CO-containing fraction to be extracted2CO of industrial tail gas2The refining and extracting system comprises a heavy component removing tower and a light component removing tower, wherein the heavy component removing tower is positioned at the front end and is connected with the light component removing tower; containing CO2The upstream gas enters a heavy component removal tower for heavy component removal treatment, wherein heavy component kettle liquid is discharged, light components enter a light component removal tower for light component removal treatment after being condensed, the light components are discharged after being treated by the light component removal tower, and the heavy components are CO2And (5) finishing.
Description
Technical Field
The utility model relates to a tail gas treatment technical field in the carbonic ester production especially relates to a contain CO2CO of industrial tail gas2A refining and extracting 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 thereof2The extraction treatment can reduce the problem of tail gas emission pollution and bring economic benefits to production enterprises, so the design provides a CO-containing material2Industrial processCO of tail gas2A refining and extracting system.
Disclosure of Invention
The utility model aims to overcome the defects of the prior art, adapt to the practical needs and provide a CO-containing material2CO of industrial tail gas2A refining and extracting system.
In order to realize the utility model discloses a purpose, the utility model discloses the technical scheme who adopts does:
design a catalyst containing CO2CO of industrial tail gas2The refining and extracting system comprises a heavy component removing tower and a light component removing tower, wherein the heavy component removing tower is positioned at the front end and is connected with the light component removing tower.
Containing CO2The upstream gas enters a heavy component removal tower for heavy component removal treatment, wherein heavy component kettle liquid is discharged, light components enter a light component removal tower for light component removal treatment after being condensed, the light components are discharged after being treated by the light component removal tower, and the heavy components are CO2And (5) finishing.
Containing CO2The upstream incoming gas is pre-cooled and then enters the de-weighting tower.
The system also comprises a heavy component removal separation tank and a heavy component removal condenser, wherein an exhaust port at the top of the heavy component removal tower is connected with an inlet of the heavy component removal condenser, an outlet of the heavy component removal condenser is connected with the heavy component removal separation tank, and a condensate outlet at the bottom of the heavy component removal separation tank is connected with an inlet at the top of the heavy component removal tower.
And the light component gas is discharged and condensed and then enters the light component removal tower.
The device also comprises a light component removal separation tank and a light component removal condenser, wherein an exhaust port at the top of the light component removal tower and an exhaust port at the top of the heavy component removal separation tank are both connected with an inlet of the light component removal condenser, an outlet of the light component removal condenser is connected with the light component removal separation tank, a condensate outlet at the bottom of the light component removal separation tank is connected with an inlet at the top of the light component removal tower, and an exhaust port at the top of the light component removal separation tank is a tail gas.
Wherein, the light component treated by the heavy component removal separation tank and the light component rectified by the light component removal tower enter a light component removal condenser to be condensed and then enter a light component removal separation tank,the condensate after the treatment of the light component removing separation tank enters the light component removing tower again for rectification, and the light component gas is discharged through a gas outlet at the top of the light component removing separation tank; the heavy component kettle liquid after rectification of the light component removal tower is CO2And (5) finishing.
And condensing the heavy component kettle liquid rectified by the light component removal tower through a cooler to form CO2And (5) finishing.
And 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, and the outlets of the heavy component removal reboiler and the light component removal reboiler are connected with an ammonia low-pressure circulating barrel.
Still include standard operating mode ammonia knockout drum, the gas vent at ammonia low pressure circulation bucket top and the access connection of standard operating mode ammonia knockout drum, the top gas vent of standard operating mode ammonia knockout drum is the ammonia discharge port, and the condensate outlet connection of standard operating mode ammonia knockout drum bottom the heat transfer medium pipe import of heavy condenser and the first heat transfer medium import of lightness condenser of taking off, the heat transfer medium pipe export of heavy condenser and the first heat transfer medium exit linkage of lightness condenser of taking off the import of standard operating mode ammonia knockout drum.
Still include low pressure ammonia knockout drum, the condensate discharge port of standard operating mode ammonia knockout drum bottom still with the access connection of this low pressure ammonia knockout drum, the import of low pressure ammonia knockout drum still is connected with low pressure ammonia supply source, the top gas vent of low pressure ammonia knockout drum is low pressure ammonia discharge port, the condensate exit linkage of low pressure ammonia knockout drum bottom the second heat transfer medium import of lightness-removing condenser, the second heat transfer medium exit linkage of lightness-removing condenser the import of low pressure ammonia knockout drum.
The condensate outlet at the bottom of the low-pressure ammonia separation tank is also connected with the heat exchange medium inlet of the subcooler, and the heat exchange medium outlet of the subcooler is connected with the inlet of the low-pressure ammonia separation tank.
The beneficial effects of the utility model reside in 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 system2Carry out and carryThe problem of direct emission and pollution of tail gas is solved, and the economic benefit of enterprises can be improved.
Drawings
Fig. 1 is a schematic diagram of the main principle of the present invention.
Detailed Description
The invention will be further described with reference to the following figures and examples:
example 1: containing CO2CO of industrial tail gas2A refined extraction system, see figure 1.
Comprises a heavy component removing tower T101 and a light component removing tower T102, wherein, the heavy component removing tower contains CO2The upstream gas enters a heavy component removal tower for heavy component removal treatment, wherein heavy component kettle liquid is discharged, light components enter a light component removal tower for light component removal treatment after being condensed, the light components are discharged after being treated by the light component removal tower, and the heavy components are CO2And (5) finishing.
The heavy component removing device comprises a heavy component removing separation tank V103 and a heavy component removing condenser E103, wherein an exhaust port at the top of the heavy component removing separation tank is connected with an inlet of the heavy component removing condenser, an outlet of the heavy component removing condenser is connected with the heavy component removing separation tank, a condensate outlet at the bottom of the heavy component removing separation tank is connected with an inlet at the top of the heavy component removing separation tank to form a cycle, light components treated by the heavy component removing separation tank enter the heavy component removing separation tank after being condensed, the condensate treated by the heavy component removing separation tank enters the heavy component removing separation tank again for rectification, and light component gases are discharged and condensed and enter the light component removing tower.
The system further comprises a light component removal separation tank V104 and a light component removal condenser E104, wherein a top exhaust port of the light component removal tower and a top exhaust port of the heavy component removal separation tank are both connected with an inlet of the light component removal condenser; wherein, the light component treated by the heavy component removal separation tank E103 and the light component rectified by the light component removal tower enter a light component removal condenser for condensation and then enter a light component removal separation tank, the condensate treated by the light component removal separation tank enters the light component removal tower again for rectification, and the light component gas is discharged through a gas outlet at the top of the light component removal separation tank; the heavy component kettle liquid after rectification of the light component removal tower is CO2And (5) finishing.
Further, the heavy component kettle liquid rectified by the light component removal tower is condensed by a cooler E105 to form the CO2And (5) finishing.
Further, in the present system, the heavy component removal reboiler E106 in the bottom of the heavy component removal column T101 and the light component removal reboiler E107 in the bottom of the light component removal column T102 are connected to ammonia gas and/or liquid ammonia, 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 tank V403.
Further, the ammonia recycling system further 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, an exhaust port at the top of the standard working condition ammonia separating tank V404A is an ammonia gas exhaust port, a condensate outlet at the bottom of the standard working condition ammonia separating tank V404A is connected with a heat exchange medium pipe inlet in the de-heavy condenser E103 and a first heat exchange medium inlet of the de-light condenser E104, 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.
Further, 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, the import of low pressure ammonia knockout drum still is connected with low pressure ammonia supply source, the top gas vent of low pressure ammonia knockout drum is low pressure ammonia discharge port, the condensate exit linkage of low pressure ammonia knockout drum bottom the second heat transfer medium import of lightness-removing condenser, the second heat transfer medium exit linkage of lightness-removing condenser the import of low pressure ammonia knockout drum, and low pressure ammonia knockout drum bottom condensate outlet still connects the heat transfer medium import of subcooler, the heat transfer medium exit linkage of subcooler the import of low pressure ammonia knockout drum.
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.
As shown in FIG. 1, the pre-cooled material contains CO2The feed gas comprises the following components:
CO295.0％、PO3.4％、N21.6％、methanol 32ppm and EO34ppm at 30 deg.C and 2.5MPa, and the heavy components are first rectified in a heavy component removing tower, and the heavy components are directly discharged to an external system for water treatment after rectification in the heavy component removing tower, wherein the temperature of the discharged heavy components is-44 deg.C and 0.5MPa, and the discharged heavy components contain CO275.63%, PO 24.34%, methanol 0.01%, EO 0.02%.
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％。
The gas separated by the heavy-weight removing separation tank and the light component discharged from the light-weight removing rectification tower enter a light-weight removing condenser together for condensation, then the condensate enters a light-weight removing separation tank for gas-liquid separation, the separated condensate enters the rectification tower again for rectification, the separated light-weight removing gas is discharged into an external system, the temperature of the light-weight removing gas is-60 ℃, the pressure of the light-weight removing gas is 5KPa, and the CO is contained265.0％、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%.
In carrying out the above-mentioned CO2During rectification and extraction, ammonia gas and liquid ammonia in an external system enter a heavy-duty reboiler E106 and a light-duty reboiler E107, ammonia passing through the heavy-duty reboiler E106 and the light-duty reboiler E107 enters an ammonia low-pressure circulation barrel, ammonia gas discharged from the ammonia low-pressure circulation barrel enters a standard working condition ammonia separation tank, gas-liquid separation is carried out in the standard working condition ammonia separation tank, light gas is discharged, condensate liquid is divided downwards into two paths and enters a heavy-duty condenser and a light-duty condenser respectively to condense the gas entering the heavy-duty condenser and the light-duty condenser, and the ammonia gas discharged from the heavy-duty condenser and the light-duty condenser enters the standard working condition ammonia separation tank again.
Meanwhile, the other part of the condenser discharged by the ammonia separating tank under the standard working condition enters the low-pressure ammonia separating tank, the condensate discharged by the low-pressure ammonia separating tank enters the subcooler and the second heat transfer pipe in the light-component removing condenser for heat exchange and then enters the low-pressure ammonia separating tank again, and the low-pressure ammonia gas discharged by the low-pressure ammonia separating tank is discharged.
So far, the CO can be completed through the system2Refining extraction and refrigeration heat exchange.
The embodiment of the present invention discloses a preferred embodiment, but not limited thereto, and those skilled in the art can easily understand the spirit of the present invention according to the above embodiment, and make different extensions and changes, but do not depart from the spirit of the present invention, all of which are within the protection scope of the present invention.
Claims (9)
1. Containing CO2CO of industrial tail gas2The refining and extracting system is characterized in that: comprises a heavy component removing tower and a light component removing tower, wherein the heavy component removing tower is positioned at the front end and is connected with the light component removing tower;
containing CO2The upstream gas enters a heavy component removal tower for heavy component removal treatment, wherein heavy component kettle liquid is discharged, light components enter a light component removal tower for light component removal treatment after being condensed, the light components are discharged after being treated by the light component removal tower, and the heavy components are CO2And (5) finishing.
2. CO-containing according to claim 12CO of industrial tail gas2The refining and extracting system is characterized in that: containing CO2The upstream incoming gas is pre-cooled and then enters the de-weighting tower.
3. CO-containing according to claim 12CO of industrial tail gas2The refining and extracting system is characterized in that: the system also comprises a heavy component removal separation tank and a heavy component removal condenser, wherein an exhaust port at the top of the heavy component removal tower is connected with an inlet of the heavy component removal condenser, an outlet of the heavy component removal condenser is connected with the heavy component removal separation tank, and a condensate outlet at the bottom of the heavy component removal separation tank is connected with an inlet at the top of the heavy component removal tower;
and the light component gas is discharged and condensed and then enters the light component removal tower.
4. CO-containing according to claim 32CO of industrial tail gas2The refining and extracting system is characterized in that: the device also comprises a light component removal separation tank and a light component removal condenser, wherein an exhaust port at the top of the light component removal tower and an exhaust port at the top of the heavy component removal separation tank are both connected with an inlet of the light component removal condenser;
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 to be condensed and then enter a light component removal separation tank, the condensate treated by the light component removal separation tank enters the light component removal tower again to be rectified, and the light component gas is discharged through a gas outlet at the top of the light component removal separation tank; the heavy component kettle liquid after rectification of the light component removal tower is CO2And (5) finishing.
5. CO-containing according to claim 42CO of industrial tail gas2The refining and extracting system is characterized in that: and condensing the heavy component kettle liquid rectified by the light component removal tower through a cooler to form CO2And (5) finishing.
6. CO-containing according to claim 52CO of industrial tail gas2The refining and extracting system is characterized in that: and 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, and the outlets of the heavy component removal reboiler and the light component removal reboiler are connected with an ammonia low-pressure circulating barrel.
7. CO-containing according to claim 62CO of industrial tail gas2The refining and extracting system is characterized in that: the ammonia low-pressure circulating barrel is characterized by further comprising a standard working condition ammonia separating tank, wherein the exhaust port at the top of the ammonia low-pressure circulating barrel is separated from the standard working condition ammoniaThe device comprises a separation tank, a standard working condition ammonia separation tank, a heat exchange medium pipe inlet of a heavy-duty condenser and a first heat exchange medium inlet of a light-duty condenser, wherein the separation tank is connected with an inlet of the separation tank, an exhaust port at the top of the standard working condition ammonia separation tank is an ammonia gas exhaust port, a condensate outlet at the bottom of the standard working condition ammonia separation tank is connected with the heat exchange medium pipe inlet of the heavy-duty condenser and the first heat exchange medium inlet of the light-duty condenser, and the heat exchange medium pipe outlet of the heavy-.
8. CO-containing according to claim 72CO of industrial tail gas2The refining and extracting system is characterized in that: still include low pressure ammonia knockout drum, the condensate discharge port of standard operating mode ammonia knockout drum bottom still with the access connection of this low pressure ammonia knockout drum, the import of low pressure ammonia knockout drum still is connected with low pressure ammonia supply source, the top gas vent of low pressure ammonia knockout drum is low pressure ammonia discharge port, the condensate exit linkage of low pressure ammonia knockout drum bottom the second heat transfer medium import of lightness-removing condenser, the second heat transfer medium exit linkage of lightness-removing condenser the import of low pressure ammonia knockout drum.
9. The CO-containing composition of claim 82CO of industrial tail gas2The refining and extracting system is characterized in that: the condensate outlet at the bottom of the low-pressure ammonia separation tank is also connected with the heat exchange medium inlet of the subcooler, and the heat exchange medium outlet of the subcooler is connected with the inlet of the low-pressure ammonia separation tank.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020751685.4U CN212893938U (en) | 2020-05-08 | 2020-05-08 | Containing CO2CO of industrial tail gas2Refining and extracting system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020751685.4U CN212893938U (en) | 2020-05-08 | 2020-05-08 | Containing CO2CO of industrial tail gas2Refining and extracting system |
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| CN212893938U true CN212893938U (en) | 2021-04-06 |
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| CN202020751685.4U Active CN212893938U (en) | 2020-05-08 | 2020-05-08 | Containing CO2CO of industrial tail gas2Refining and extracting system |
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