CN111569593A - Carbon dioxide, epoxypropane extraction refining system in carbonic ester production tail gas - Google Patents
Carbon dioxide, epoxypropane extraction refining system in carbonic ester production tail gas Download PDFInfo
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- CN111569593A CN111569593A CN202010383714.0A CN202010383714A CN111569593A CN 111569593 A CN111569593 A CN 111569593A CN 202010383714 A CN202010383714 A CN 202010383714A CN 111569593 A CN111569593 A CN 111569593A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D301/00—Preparation of oxiranes
- C07D301/32—Separation; Purification
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D303/00—Compounds containing three-membered rings having one oxygen atom as the only ring hetero atom
- C07D303/02—Compounds containing oxirane rings
- C07D303/04—Compounds containing oxirane rings containing only hydrogen and carbon atoms in addition to the ring oxygen atoms
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/704—Solvents not covered by groups B01D2257/702 - B01D2257/7027
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
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Abstract
The invention discloses a system for extracting and refining carbon dioxide and epoxypropane in tail gas in carbonate production, which comprises a compression precooling system, a CO (carbon monoxide) system and a CO system which are sequentially connected in series2An extraction refining system, a propylene oxide 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 rectifies and separates the precooled feed gas or/and condensate to obtain finished product CO2(ii) a By CO2The tail gas discharged after rectification of the extraction and refining system enters a propylene oxide refining system for rectification and separation to obtain a finished product of propylene oxide, wherein the CO is2And the residual liquid and the residual gas treated by the extraction refining system and the propylene oxide refining system enter the discharge system.
Description
Technical Field
The invention relates to the technical field of tail gas treatment in carbonate production, in particular to a system for extracting and refining carbon dioxide and epoxypropane in the tail gas in the carbonate production.
Background
In a carbonate production system, the off-gas produced in its production contains a large amount of CO2And high pollution and toxic gases such as propylene oxide, etc., andCO in the exhaust gas2Propylene oxide, etc. are also commonly used industrial raw materials, and thus, for example, CO in its tail gas2The problem of tail gas emission pollution can be reduced by extracting and treating the propylene oxide, and economic benefits can be brought to production enterprises.
Disclosure of Invention
The invention aims to overcome the defects of the prior art, adapt to the practical requirements and provide a system for extracting and refining carbon dioxide and propylene oxide in the tail gas in the production of carbonic ester.
In order to realize the purpose of the invention, the technical scheme adopted by the invention is as follows:
discloses a system for extracting and refining carbon dioxide and propylene oxide in tail gas in the production of carbonic ester, which comprises a compression precooling system, a CO (carbon monoxide) system and a CO system which are sequentially connected in series2An extraction refining system, a propylene oxide 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 rectifies and separates the precooled feed gas or/and condensate to obtain finished product CO2(ii) a By CO2The tail gas discharged after rectification of the extraction and refining system enters a propylene oxide refining system for rectification and separation to obtain a finished product of propylene oxide, wherein the CO is2And the residual liquid and the residual gas treated by the extraction refining system and the propylene oxide 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 the precooler is connected with the carbon dioxide compressor front separation tank.
The upstream incoming gas and the raw material containing the propylene oxide enter the carbon dioxide buffer tank through an inlet pipe, 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, 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 a discharge system, the other path is connected with the air inlet of the carbon dioxide compressor, the liquid outlet at the bottom of the front separation tank of the carbon dioxide compressor is connected with a propylene oxide condensate pump, and the outlet of the propylene oxide condensate pump is connected with a propylene oxide refining system.
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 carbon dioxide separating tank, 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.
The CO is2The extraction and refining system comprises a heavy component removing tower, a light component removing tower, a heavy component removing separating tank, a heavy component removing condenser, a light component removing separating tank and a light component removing condenser.
And 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 condensed2And putting the finished product into a storage tank.
And 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 outlet 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 carbon dioxide separation tank, a liquid outlet at the bottom of the carbon dioxide separation tank is connected with a discharge system, and an exhaust port at the top of the carbon dioxide separation tank is connected with a carbon dioxide buffer tank.
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 in a refrigerating 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 ammonia low-pressure circulation device is characterized by further comprising a standard working condition ammonia separation tank, 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, an exhaust port at the top of the standard working condition ammonia separation tank is an ammonia gas exhaust port and enters a 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 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 separation.
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.
The propylene oxide extraction and refining system comprises a degassing tower, a propylene oxide rectifying tower and a carbon dioxide separation tank, wherein a liquid outlet at the bottom of the degassing tower is connected with the propylene oxide rectifying tower through a degassing kettle liquid pump.
The system comprises a propylene oxide rectifying tower, a degassing condenser, a degassing separator, a degassing condenser inlet, a degassing condenser outlet, a catalytic combustion device and a liquid outlet at the bottom of the degassing separator, wherein the outlet of the propylene oxide condensate pump is connected with the propylene oxide rectifying tower, the degassing condenser outlet is connected with the degassing condenser inlet, the degassing separator outlet is connected with the catalytic combustion device, and the liquid outlet at the bottom of the degassing separator is connected with the top of the degassing tower.
Still include propylene oxide condenser, propylene oxide separator, wherein, the gas vent and the propylene oxide condenser access connection at propylene oxide rectifying column top, propylene oxide condenser export with propylene oxide separator access connection, the leakage fluid dram of propylene oxide separator divide into two the tunnel, wherein all the way with propylene oxide rectifying column top is connected, and another the tunnel is the export of propylene oxide finished product and is connected with a propylene oxide pump, and the export of propylene oxide pump divide into two the tunnel, wherein is connected with propylene oxide pump storage tank all the way, and another the tunnel is connected with the propylene oxide separator.
An outlet at the top of the propylene oxide separator is connected with a tail gas treatment device; the tail gas treatment device comprises a vacuum fan and a water seal tank, wherein an outlet at the top of the epoxypropane separator is connected with an inlet of the vacuum fan, an outlet of the vacuum fan is connected with an air inlet of the water seal tank, and a nitrogen inlet is formed in a pipeline between the vacuum fan and the epoxypropane separation tank.
The gas vent and the catalytic combustion device at water seal tank top are connected, water seal tank bottom leakage fluid dram is connected with the collection liquid jar among the discharge system, be equipped with a condenser pipe in the water seal tank, the condenser pipe import is connected with the liquid ammonia among the refrigerating system, and the condenser pipe export is connected with the heavy reboiler that takes off.
And a liquid outlet at the bottom of the epoxypropane rectifying tower is connected with a propylene carbonate pump, an outlet of the propylene carbonate pump is divided into two paths, one path is a waste liquid discharge pipe, and the other path is communicated with the inside of the epoxypropane rectifying tower.
And the inlet of a degassing reboiler in the degassing tower and the inlet of a propylene oxide reboiler in the propylene oxide rectifying tower are both connected with a heat-conducting medium supply main pipe, and the outlet of the degassing reboiler in the degassing tower and the outlet of the propylene oxide reboiler in the propylene oxide rectifying tower are connected with a heat-conducting medium reflux main pipe.
Still include standard ammonia knockout drum, the gas vent at low pressure circulation bucket top is connected standard ammonia knockout drum import, the leakage fluid dram of standard ammonia knockout drum bottom divide into two the tunnel, wherein connect all the way import of the heat-transfer pipe in the degasification condenser, another way is connected import of the heat-transfer pipe in the epoxypropane, export of the heat-transfer pipe in the degasification condenser and import of the exit linkage standard ammonia knockout drum of heat-transfer pipe in the epoxypropane condenser.
Further comprises a compression pre-cooling system and a CO2Extract the refrigerating system that refined system, epoxypropane extract refined system, discharge system provided the energy, refrigerating system includes liquid storage pot, supplementary liquid storage pot, ammonia gas 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; the top of the liquid storage tank and the auxiliary liquid storage tank is provided with an ammonia gas exhaust pipe 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 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.
And the ammonia gas discharged from the 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, the outlet of the heat transfer pipe in the ammonia gas cooler is connected with the inlet of a heavy component removal reboiler in the 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 ammonia gas cooler is connected with a circulating water return main pipe.
And the liquid outlet of the liquid storage tank is connected with the inlet of the condensing pipe.
And the ammonia gas exhaust pipes at the tops of the liquid ammonia liquid storage tank and the auxiliary liquid storage tank are also connected with a discharge system.
The exhaust port at the top of the standard ammonia separation tank and the exhaust port at the top of the standard ammonia separation tank enter the standard working condition ice machine together; and the outlet of the ice machine under the standard working condition and the exhaust port of the auxiliary liquid storage tank are connected with the air inlet of the ammonia evaporative condenser.
Discharge system includes buffer tank, tail gas water seal jar, collection liquid jar, the buffer tank be equipped with high-pressure gas advance the pipe and with the ammonia blast pipe at liquid ammonia 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.
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 a liquid collection tank, and a submerged pump is arranged in the liquid collection tank and discharges liquid in the liquid collection tank.
The invention has the beneficial effects that:
the carbon dioxide and propylene oxide extracting and refining system in the carbonic ester production tail gas can be used for extracting and refining CO in the tail gas treatment system2And the propylene oxide is extracted, so that the problem of direct emission pollution of tail gas can be solved, and 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 diagram of the main principle of a propylene oxide refining system according to the present invention;
fig. 5 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: a system for extracting and refining carbon dioxide and propylene oxide in tail gas in the production of carbonic ester is disclosed, and refer to figures 1 to 5.
Comprises a compression precooling system and CO which are connected in series in sequence2An extraction refining system, a propylene oxide 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 rectifies and separates the precooled feed gas or/and condensate to obtain finished product CO2(ii) a By CO2The tail gas discharged after rectification of the extraction and refining system enters a propylene oxide refining system for rectification and separation to obtain a finished product of propylene oxide, wherein the CO is2And the residual liquid and the residual gas treated by the extraction refining system and the propylene oxide 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 incoming gas (raw material gas) and the raw material containing the propylene oxide enter the carbon dioxide buffer tank through an inlet pipe 201, 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, 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 a discharge system, the other path is connected with the air inlet of the carbon dioxide compressor, the liquid outlet at the bottom of the front separation tank of the carbon dioxide compressor is connected with a propylene oxide condensate pump, and the outlet of the propylene oxide condensate pump is connected with a propylene oxide refining system.
The exhaust port of the carbon dioxide compressor is connected with the air inlet of the carbon dioxide after-cooler, and the exhaust port at the top of the carbon dioxide after-cooler enters the air inlet of the carbon dioxide after-separating tankIn the mouth, the condensate discharge port at the bottom of the carbon dioxide post-separation tank is connected with the carbon dioxide separation tank, and the exhaust port at the top of the carbon dioxide post-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.
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 enters a heavy component removal tower from an air outlet at the top of the separation tank for heavy component removal treatment, wherein heavy component kettle liquid enters the precooler through a liquid discharge pipe 1102 at the bottom, light components enter the heavy component removal separation tank through an exhaust pipe and are condensed in the heavy component removal condenser, 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 condensed2And putting the finished product into a storage tank.
And 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 103 of the first heat exchange tube in the precooler is emptied.
And a liquid outlet 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 carbon dioxide separation tank, a liquid outlet at the bottom of the carbon dioxide separation tank is connected with a discharge system, and an exhaust port at the top of the carbon dioxide separation tank is connected with a carbon dioxide buffer tank.
Furthermore, the heavy component removal reboiler E106 in the bottom of the heavy component removal tower and the light component removal reboiler E107 in the bottom of the light component removal tower in the system are connected with ammonia gas or/and liquid ammonia in the refrigeration system, and the outlets of the heavy component removal reboiler and the light component removal reboiler are connected with an ammonia low-pressure circulation barrel V403.
The ammonia low-pressure circulating tank is characterized by further comprising 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 a 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.
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.
Specifically, the propylene oxide extraction and purification system comprises a degassing tower T201, a propylene oxide rectifying tower T202 and a carbon dioxide separation tank V201, wherein a liquid outlet at the bottom of the degassing tower is connected with the propylene oxide rectifying tower T202 through a degassing kettle pump P202A.
The exit linkage of epoxypropane condensate pump still includes degasification condenser E201, degasification separator V202, degasification tower top gas vent with degasification condenser access connection, degasification condenser export with degasification separator access connection, degasification separator gas vent 2802 is connected with catalytic combustion device, degasification separator bottom leakage fluid dram is connected with the degasification tower top.
Still include propylene oxide condenser E202, propylene oxide separator V203, wherein, the gas vent and the propylene oxide condenser access connection at propylene oxide rectifying column top, propylene oxide condenser export with propylene oxide separator access connection, the leakage fluid dram of propylene oxide separator divide into two the tunnel, wherein all the way with propylene oxide rectifying column top is connected, and another way is the export of propylene oxide finished product and is connected with a propylene oxide pump P203A, and the export of propylene oxide pump divide into two the tunnel, wherein 205 and propylene oxide pump storage tank are connected all the way, and another way is connected with the propylene oxide separator.
An outlet at the top of the propylene oxide separator is connected with a tail gas treatment device; tail gas processing apparatus includes vacuum fan C201, water sealed tank V204, wherein, epoxypropane separator top export and vacuum fan access connection, vacuum fan export and water sealed tank air inlet are connected be equipped with nitrogen gas access mouth on the pipeline between vacuum fan and the epoxypropane separator, can import nitrogen gas to tail gas processing apparatus through this nitrogen gas access mouth, through combustible gas content in this nitrogen gas reduction tail gas, improve entire system security.
The gas vent and the catalytic combustion device at water seal tank top are connected, water seal tank bottom leakage fluid dram is connected with the collection liquid jar among the discharge system, be equipped with a condenser pipe in the water seal tank, the condenser pipe import is connected with the liquid ammonia among the refrigerating system, and the condenser pipe export is connected with the heavy reboiler that takes off.
Furthermore, a liquid outlet at the bottom of the propylene oxide rectifying tower is connected with a propylene carbonate pump P204, an outlet of the propylene carbonate pump P204 is divided into two paths, wherein one path 204 is a waste liquid discharge pipe, and the other path inputs propylene oxide into the propylene oxide rectifying tower again through the propylene carbonate pump P204.
The inlet of a degassing reboiler E203 in the degassing tower and the inlet of a propylene oxide reboiler E204 in the propylene oxide rectifying tower are both connected with a heat-conducting medium supply main pipe 602, and the outlet of the degassing reboiler in the degassing tower and the outlet of the propylene oxide reboiler in the propylene oxide rectifying tower are connected with a heat-conducting medium reflux main pipe 601.
The ammonia low-pressure circulating tank is characterized by further comprising a standard ammonia separating tank V404B, wherein a gas outlet 4201 at the top of the ammonia low-pressure circulating barrel is connected with an inlet of the standard ammonia separating tank, a liquid outlet at the bottom of the standard ammonia separating tank is divided into two paths, one path of liquid outlet is connected with an inlet of a heat transfer pipe in the degassing condenser, the other path of liquid outlet is connected with an inlet of a heat transfer pipe in the propylene oxide condenser, and an outlet of the heat transfer pipe in the degassing condenser and an outlet of the heat transfer pipe in the propylene oxide condenser are.
Further comprises a compression pre-cooling system and a CO2Extract the refrigerating system that refined system, epoxypropane extracted refined system, discharge system provided the energy, it is further, epoxypropane rectifying column bottom leakage fluid dram is connected with carbonic propylene pump P204, carbonic propylene pump P204 export is divided into two routes, and wherein one is the waste liquid discharge pipe, and inside another way inputed epoxypropane to the epoxypropane rectifying column once more through this carbonic propylene pump P204, 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 also 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.
CO2And ammonia gas discharged from a top exhaust port 4401 of an ammonia separation tank under the standard working condition in an extraction and refining system and an exhaust port 2401 of an ammonia separation tank under the standard working condition in a propylene oxide refining system passes through an ice maker under the standard working condition and then enters an ammonia gas inlet of the ammonia evaporative condenser together with an ammonia gas exhaust port at the top of the auxiliary liquid storage tank.
Further, ammonia gas discharged from an exhaust port 4402 at the top of the low-pressure ammonia separation tank enters a 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 4103 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, ammonia blast pipe 402 at liquid ammonia 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 ammonia 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 outlet 1903 at the bottom of the carbon dioxide buffer tank and a liquid outlet 201 at the bottom of the carbon dioxide separation tank 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 outlet pipe 904 on the submerged pump.
The liquid storage tank V402 is also connected with the inlet of the condensation pipe in the water sealing tank through a liquid discharge pipe 4202.
Particularly, discharge system includes buffer tank V901, tail gas water-sealed tank 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 ammonia liquid storage pot and supplementary liquid storage pot top is connected, the blast pipe at buffer tank top is connected with the air inlet on the tail gas water-sealed tank.
Further, the liquid outlet 1903 at the bottom of the carbon dioxide buffer tank, the liquid outlet 201 at the bottom of the carbon dioxide separation tank and the liquid outlet at the bottom of the water seal tank are connected with the liquid collection tank, a submerged pump P901 is arranged in the liquid collection tank, and the liquid in the liquid collection tank is discharged through a liquid outlet 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 feed gas 1 (feed gas 1) was as follows:
the temperature is 15 ℃ and 3 KP.
The composition of the upstream feed gas 2 (feed gas 2) was as follows:
| name (R) | CO2 | C2H4O |
| Volume fraction | 99.95％ | 0.05％ |
The temperature is 8 ℃ and 3 KP.
The two streams of upstream incoming gas firstly enter 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 C24.3% of PO, 0.2% of methanol, 0.7% of allyl alcohol, 0.9% of propylene glycol and 0.02% of EO, and contains much carbon dioxideThe gas enters the carbon dioxide compressor C102, and the gas compressed by the carbon dioxide compressor C102 enters the rear carbon dioxide cooler E102.
The carbon dioxide cooler E102 is a water-cooled cooler, the inlet and the outlet of a heat exchange tube in the carbon dioxide cooler E102 are respectively connected with a circulating water inlet manifold 501 and a circulating water return manifold 502, and the gas treated by the carbon dioxide cooler E102 is discharged and enters CO2In the extraction and refining system, the condensate is discharged into a carbon dioxide post-separation tank, and CO in the condensate2The content is 37.0 percent, so that the pre-cooling treatment of the tail gas can be completed.
In CO2Extracting CO from the gas entering the refining system295.0 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 carbon dioxide separation tank after passing through a precooler, the carbon dioxide separation tank 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％。
The gas separated by the heavy-weight removing separation tank and the light component discharged from the light-weight removing rectification tower are fed into a light-weight removing condenser together for condensation, then the condensate is fed into the light-weight removing separation tank for gas-liquid separation, the separated condensate is fed into the light-weight removing tower again for rectification, the separated light-weight removing gas is discharged into a precooler and then discharged, the temperature of the light-weight removing gas is-60 ℃, the pressure of the light-weight removing gas is 5KPa, and the light-weight removing gas contains CO265.0％、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%.
Liquid discharged from a front separation tank of a carbon dioxide compressor is input into the carbon dioxide separation tank through a liquid outlet 1201 of a propylene oxide condensate pump and then input into a light component removal tower, the raw material gas containing propylene oxide has the temperature of 30 ℃ and 0.3MPa, contains 20 percent of PO (propylene oxide) and 80 percent of propylene carbonate, firstly, the carbon dioxide enters a carbon dioxide separation tank for gas-liquid separation, flash steam is discharged through an exhaust pipe 2101, the liquid enters a degassing tower, the light components treated by the degassing tower enter a degassing condenser to be condensed and then enter a degassing separator to be subjected to gas-liquid separation, the gas separated by the degassing separator is discharged into a catalytic combustion device to be subjected to catalytic combustion, the temperature of the gas separated by the degassing separator is-12 ℃, 3KP, the content of carbon dioxide is 87.7 percent, and the content of PO (propylene oxide) is 0.2 percent, and the condensate separated by the degassing separator enters the degassing tower again to be rectified.
The heavy still liquid discharged from the degassing tower is input into the propylene oxide rectifying tower through a degassing still liquid pump for rectification again, the heavy still liquid discharged from the propylene oxide rectifying tower is a mixed material and is discharged to an external system through a discharge pipe 204 for water treatment, the other part of the mixed material enters the propylene oxide rectifying tower again for rectification treatment, and the heavy still liquid discharged from the propylene oxide rectifying tower has the temperature of 27 ℃, 0.08MPa, 16.0 percent of PO (propylene oxide), 82.4 percent of propylene carbonate, 0.2 percent of methanol, 0.6 percent of propylene alcohol and 0.8 percent of propylene glycol.
The light component discharged from the epoxypropane rectifying tower enters an epoxypropane condenser for condensation and then enters an epoxypropane separator for gas-liquid separation, wherein one part of condensate discharged from the epoxypropane separator enters the epoxypropane rectifying tower for rectification again, the other part of condensate is divided into two paths by an epoxypropane pump, one path of condensate enters the epoxypropane separator again, the other part of condensate is a epoxypropane finished product and enters an epoxypropane storage tank through a liquid discharge pipe 205, the temperature of the epoxypropane finished product is-4 ℃, 0.08MPa, the epoxypropane finished product contains 99.7 percent of PO (epoxypropane) and 0.3 percent of propylene carbonate.
The gas discharged from the epoxypropane separator enters a water seal tank through a vacuum fan and is absorbed by the solvent, a condenser pipe is arranged in the water seal tank, the inlet of the condenser pipe is connected with a liquid storage tank, the outlet 2402 of the condenser pipe is used for introducing ammonia gas into an ammonia low-pressure circulating barrel, and the liquid ammonia enters the condenser pipe to improve the absorption of the solvent in the water seal tank on the gas in the tail gas.
The mass transfer and heat exchange process of the system is as follows:
in the mass transfer and heat exchange of the propylene oxide extraction and purification system, liquid ammonia from the liquid storage tank enters a standard ammonia separation tank V404B, the liquid enters a heat transfer pipe in a degassing condenser and a heat transfer pipe in a propylene oxide condenser for condensation, the outlet of the liquid ammonia and the outlet of the heat transfer pipe of the propylene oxide condenser enter the standard ammonia separation tank again, and the liquid ammonia is discharged from an exhaust port 2401 of the standard ammonia separation tank.
In the refrigeration system, 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 lightness-removing reboiler, enters an ammonia low-pressure circulating barrel after passing through the lightness-removing reboiler, ammonia in the liquid storage tank enters a lightness-removing reboiler E107, the ammonia passing through a weight-removing reboiler E106 and the lightness-removing reboiler E107 enters an ammonia low-pressure circulating barrel, the ammonia discharged through 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 then 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, epoxypropane refining extraction, refrigeration heat exchange and tail gas emission.
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 (10)
1. A carbon dioxide, epoxypropane extraction refining system in carbonic ester production tail gas which characterized in that: comprises a compression precooling system and CO which are connected in series in sequence2An extraction refining system, a propylene oxide 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 rectifies and separates the precooled feed gas or/and condensate to obtain finished product CO2(ii) a By CO2The tail gas discharged after the rectification of the extraction and refining system enters into the epoxyRectifying in a propane refining system to separate out the finished product of propylene oxide, wherein the CO is2And the residual liquid and the residual gas treated by the extraction refining system and the propylene oxide refining system enter the discharge system.
2. The system for extracting and refining carbon dioxide and propylene oxide in the tail gas of carbonate production according to claim 1, wherein: 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 incoming gas and the raw material containing the propylene oxide enter the carbon dioxide buffer tank through an inlet pipe, 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, 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 a discharge system, the other path is connected with the air inlet of the carbon dioxide compressor, the liquid outlet at the bottom of the front separation tank of the carbon dioxide compressor is connected with a propylene oxide condensate pump, and the outlet of the propylene oxide condensate pump is connected with a propylene oxide refining system;
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 carbon dioxide separating tank, 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. The system for extracting and refining carbon dioxide and propylene oxide in the tail gas of carbonate production according to claim 2, wherein: the CO is2The extraction and refining system comprises a heavy component removing tower, a light component removing tower, a heavy component removing separating tank, a heavy component removing condenser, a light component removing separating 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 outlet 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 carbon dioxide separation tank, a liquid outlet at the bottom of the carbon dioxide separation tank is connected with a discharge system, and an exhaust port at the top of the carbon dioxide separation tank is connected with a carbon dioxide buffer tank.
4. The system for extracting and refining carbon dioxide and propylene oxide in the tail gas of carbonate production according to claim 3, wherein: 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. The system for extracting and refining carbon dioxide and propylene oxide in the tail gas of carbonate production according to claim 4, wherein: the propylene oxide extraction and refining system comprises a degassing tower, a propylene oxide rectifying tower and a carbon dioxide separation tank, wherein a liquid outlet at the bottom of the degassing tower is connected with the propylene oxide rectifying tower through a degassing kettle liquid pump;
the outlet of the epoxypropane condensate pump is connected with the epoxypropane rectifying tower, the epoxypropane rectifying tower further comprises a degassing condenser and a degassing separator, the exhaust port at the top of the degassing tower is connected with the inlet of the degassing condenser, the outlet of the degassing condenser is connected with the inlet of the degassing separator, the exhaust port of the degassing separator is connected with a catalytic combustion device, and the liquid outlet at the bottom of the degassing separator is connected with the top of the degassing tower;
still include propylene oxide condenser, propylene oxide separator, wherein, the gas vent and the propylene oxide condenser access connection at propylene oxide rectifying column top, propylene oxide condenser export with propylene oxide separator access connection, the leakage fluid dram of propylene oxide separator divide into two the tunnel, wherein all the way with propylene oxide rectifying column top is connected, and another the tunnel is the export of propylene oxide finished product and is connected with a propylene oxide pump, and the export of propylene oxide pump divide into two the tunnel, wherein is connected with propylene oxide pump storage tank all the way, and another the tunnel is connected with the propylene oxide separator.
6. The system for extracting and refining carbon dioxide and propylene oxide in the tail gas of carbonate production according to claim 5, wherein: an outlet at the top of the propylene oxide separator is connected with a tail gas treatment device; the tail gas treatment device comprises a vacuum fan and a water seal tank, wherein an outlet at the top of the epoxypropane separator is connected with an inlet of the vacuum fan, an outlet of the vacuum fan is connected with an air inlet of the water seal tank, and a nitrogen inlet is arranged on a pipeline between the vacuum fan and the epoxypropane separation tank;
an exhaust port at the top of the water seal tank is connected with a catalytic combustion device, a liquid discharge port at the bottom of the water seal tank is connected with a liquid collection tank in a discharge system, a condenser pipe is arranged in the water seal tank, an inlet of the condenser pipe is connected with liquid ammonia in a refrigeration system, and an outlet of the condenser pipe is connected with a heavy component removal reboiler;
and a liquid outlet at the bottom of the epoxypropane rectifying tower is connected with a propylene carbonate pump, an outlet of the propylene carbonate pump is divided into two paths, one path is a waste liquid discharge pipe, and the other path is communicated with the inside of the epoxypropane rectifying tower.
7. The system for extracting and refining carbon dioxide and propylene oxide in the tail gas of carbonate production according to claim 6, wherein: an inlet of a degassing reboiler in the degassing tower and an inlet of a propylene oxide reboiler in the propylene oxide rectifying tower are both connected with a heat-conducting medium supply main pipe, and an outlet of the degassing reboiler in the degassing tower and an outlet of the propylene oxide reboiler in the propylene oxide rectifying tower are connected with a heat-conducting medium reflux main pipe;
still include standard ammonia knockout drum, the gas vent at low pressure circulation bucket top is connected standard ammonia knockout drum import, the leakage fluid dram of standard ammonia knockout drum bottom divide into two the tunnel, wherein connect all the way import of the heat-transfer pipe in the degasification condenser, another way is connected import of the heat-transfer pipe in the epoxypropane, export of the heat-transfer pipe in the degasification condenser and import of the exit linkage standard ammonia knockout drum of heat-transfer pipe in the epoxypropane condenser.
8. The system for extracting and refining carbon dioxide and propylene oxide in the tail gas of carbonate production according to claim 7, wherein: further comprises a compression pre-cooling system and a CO2Extract the refrigerating system that refined system, epoxypropane extract refined system, discharge system provided the energy, refrigerating system includes liquid storage pot, supplementary liquid storage pot, ammonia gas 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, an outlet of the heat transfer pipe in the ammonia gas cooler is connected with an inlet of a heavy component removal reboiler in a 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 ammonia gas cooler is connected with a circulating water return main pipe;
the liquid outlet of the liquid storage tank is connected with the inlet of the condensing pipe;
and the ammonia gas exhaust pipes at the tops of the liquid ammonia liquid storage tank and the auxiliary liquid storage tank are also connected with a discharge system.
9. The system for extracting and refining carbon dioxide and propylene oxide in the tail gas of carbonate production according to claim 8, wherein: the exhaust port at the top of the standard ammonia separation tank and the exhaust port at the top of the standard ammonia separation tank enter the standard working condition ice machine together; and the outlet of the ice machine under the standard working condition and the exhaust port of the auxiliary liquid storage tank are connected with the air inlet of the ammonia evaporative condenser.
10. The system for extracting and refining carbon dioxide and propylene oxide from carbonate production tail gas according to claim 9, wherein: the discharge system comprises a buffer tank, a tail gas water seal tank and a liquid collection tank, wherein the buffer tank is provided with a high-pressure gas inlet pipe and is connected with the liquid ammonia 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 collection 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;
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 a liquid collection tank, and a submerged pump is arranged in the liquid collection tank and discharges liquid in the liquid collection tank.
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