CN111256432B - Device and method for treating waste liquid from carbon dioxide rectification separation - Google Patents
Device and method for treating waste liquid from carbon dioxide rectification separation Download PDFInfo
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- CN111256432B CN111256432B CN202010170999.XA CN202010170999A CN111256432B CN 111256432 B CN111256432 B CN 111256432B CN 202010170999 A CN202010170999 A CN 202010170999A CN 111256432 B CN111256432 B CN 111256432B
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- 239000007788 liquid Substances 0.000 title claims abstract description 198
- 238000000926 separation method Methods 0.000 title claims abstract description 119
- 239000002699 waste material Substances 0.000 title claims abstract description 77
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 70
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 35
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 33
- 238000000034 method Methods 0.000 title claims description 26
- 239000007789 gas Substances 0.000 claims abstract description 159
- 239000012071 phase Substances 0.000 claims abstract description 41
- 239000002994 raw material Substances 0.000 claims abstract description 37
- 239000007791 liquid phase Substances 0.000 claims abstract description 33
- 239000002912 waste gas Substances 0.000 claims abstract description 11
- 238000009833 condensation Methods 0.000 claims description 17
- 230000005494 condensation Effects 0.000 claims description 17
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 238000010992 reflux Methods 0.000 claims description 3
- 238000001816 cooling Methods 0.000 description 7
- 230000006837 decompression Effects 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 238000002309 gasification Methods 0.000 description 6
- 238000012546 transfer Methods 0.000 description 5
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000020335 dealkylation Effects 0.000 description 1
- 238000006900 dealkylation reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0266—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon dioxide
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
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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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Carbon And Carbon Compounds (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention discloses a device for treating waste liquid generated by rectifying and separating carbon dioxide, which relates to the technical field of rectifying and separating carbon dioxide, and comprises the following components: a gas compressor; the inlet of the heavy-removal tower is connected with the gas compressor; the inlet of the first gas-liquid separation device is connected with a steam outlet at the top of the heavy-removal tower; the inlet of the second gas-liquid separation device is connected with the gas phase outlet of the first gas-liquid separation device; the inlet of the light component removing tower is connected with the liquid phase outlet of the second gas-liquid separation device; the heat exchanger is provided with a raw material gas inlet, a raw material gas outlet, a waste liquid inlet and a waste gas outlet, wherein the waste liquid inlet is connected with a waste liquid outlet at the bottom of the heavy-removal tower, and the raw material gas outlet is connected with a gas inlet of the gas compressor; and the buffer tank is connected with the waste gas outlet of the heat exchanger and is also connected with the gas phase outlet of the second gas-liquid separation device. According to the invention, the raw material gas exchanges heat with the heavy component waste liquid from the bottom of the heavy component removal tower, so that the cold energy of the waste liquid is recycled, the yield of the system is improved, and the purposes of saving energy and increasing yield are achieved.
Description
Technical Field
The invention relates to the technical field of carbon dioxide rectification separation, in particular to a device and a method for treating waste liquid generated in carbon dioxide rectification separation.
Background
With the rapid development of industry, CO as a main greenhouse gas 2 The annual emission of (2) is increased, which is worry, and at the same time, CO2 has extremely wide application in the fields of industry, agriculture, food, medicine, fine chemical industry and the like, and CO2 is recovered from byproduct gas sources of various industrial processes, so that carbon resources can be comprehensively utilized, and environmental pollution caused by industrial waste gas emission can be treated.
Currently, the industrial production of carbon dioxide mainly utilizes industrial carbon-containing waste gas (CO 2 Content > 80%) by separation. In addition to CO contained in the exhaust gas 2 In addition, H is contained 2 S、COS、C 2 H 4 、C 2 H 6 、C 3 H 6 、C 6 H 6 、CH 3 OH and other impurities. There are generally two methods for separating these impurities, one is to remove H first by physical or chemical adsorption 2 S, then through oxidation combustion, the organic hydrocarbon is converted into H 2 O、CO 2 Wherein, the adsorbent is used for many times and then is used as dangerous solid waste for landfill, and the catalyst for oxidative dealkylation is also refined and then is used for landfill after long-time use. Secondly, by a rectification process, the components are discharged from the bottom of the heavy-removal tower by utilizing the difference of relative volatilities and collected and then concentrated for treatment.
However, a great amount of waste liquid is generated in the carbon dioxide rectification separation process, the waste liquid is discharged from the bottom of the heavy-removal tower, the temperature is lower than-12 ℃, and the sulfur and benzene contents in the waste liquid exceed the standard, so that the collection, storage and treatment of the waste liquid are very inconvenient, and the waste liquid treatment becomes a great difficulty in the process.
Disclosure of Invention
The invention aims at: the utility model provides a carbon dioxide rectification separation waste liquid treatment device and method, through the heat transfer of raw materials gas and heavy ends waste liquid from the heavy ends tower bottom, make the cold energy recycle of waste liquid, reach the effect of energy recovery, the energy saving, thereby the raw materials gas cooling is absorbed in the process of gasification, decompression in the heat exchanger to waste liquid simultaneously, the cooling of raw materials gas can make gas compressor's air input increase, thereby improved the throughput of system, increased the output of follow-up liquid carbon dioxide, reach the purpose of increasing production.
The technical scheme adopted by the invention is as follows:
in order to achieve the above object, the present invention provides a device for treating waste liquid from carbon dioxide rectification separation, comprising:
the gas compressor compresses the gas and sends the compressed gas to a subsequent rectification separation process;
the inlet of the heavy-removal tower is connected with a gas compressor, steam is discharged from the top of the heavy-removal tower, a reboiler is arranged at the bottom of the heavy-removal tower, liquid is gasified by the reboiler, and the residual liquid is discharged as heavy component waste liquid;
the inlet of the first gas-liquid separation device is connected with a steam outlet at the top of the heavy-removal tower;
the inlet of the second gas-liquid separation device is connected with the gas phase outlet of the first gas-liquid separation device; the first gas-liquid separation device condenses and separates gas and liquid from the vapor discharged from the top of the heavy removal tower, the separated liquid phase flows back into the heavy removal tower, the gas phase enters the second gas-liquid separation device to be condensed and separated again, the separated gas phase is non-condensable tail gas, the separated liquid phase enters the light removal tower to be rectified and separated, the gas phase separated by the light removal tower is mixed with the gas before entering the second gas-liquid separation device, and the second condensation and gas-liquid separation operation is circularly carried out, so that the separation is more thorough, the product purity is improved, and the high-purity liquid carbon dioxide can be obtained from the bottom of the light removal tower;
the inlet of the light component removing tower is connected with the liquid phase outlet of the second gas-liquid separation device, the bottom liquid is gasified by the reboiler part, and the rest liquid is subjected to a cooler to obtain liquid carbon dioxide;
the heat exchanger is provided with a raw material gas inlet, a raw material gas outlet, a waste liquid inlet and a waste gas outlet, wherein the waste liquid inlet is connected with a waste liquid outlet at the bottom of the heavy component removal tower, the raw material gas outlet is connected with a gas compressor air inlet, raw material gas enters the heat exchanger to exchange heat with heavy component waste liquid from the heavy component removal tower, and the waste liquid absorbs a large amount of heat in the process of gasification and decompression in the heat exchanger so as to cool the raw material gas, and the cooled raw material gas enters the gas compressor again, so that the air inflow of the gas compressor can be increased through cooling the raw material gas, the treatment capacity of the system is improved, and the yield of the subsequent liquid carbon dioxide is increased; and
And the buffer tank is connected with the waste gas outlet of the heat exchanger and is connected with the gas phase outlet of the second gas-liquid separation device, the waste liquid is gasified after entering the heat exchanger, is discharged from the waste gas outlet of the heat exchanger and enters the buffer tank to be mixed with non-condensable tail gas from the gas phase outlet of the second gas-liquid separation device, and is emptied after reaching the standard.
Working principle:
the method comprises the steps of feeding raw gas into a heat exchanger to exchange heat with heavy component waste liquid from the bottom of a heavy component removal tower, absorbing a large amount of heat in the process of gasifying and decompressing the waste liquid in the heat exchanger so as to cool the raw gas, feeding the cooled raw gas into a gas compressor, compressing the cooled raw gas, feeding the compressed raw gas into the heavy component removal tower for rectification separation, condensing the separated steam through a first gas-liquid separation device and separating gas from liquid to obtain gas phase and liquid phase, feeding the liquid phase condensate back into the heavy component removal tower, exchanging heat with the raw gas, recycling cold energy of the waste liquid, and cooling the waste liquid.
The gas phase separated by the first gas-liquid separation device enters the second gas-liquid separation device for condensation and gas-liquid separation, the separated gas phase is used as non-condensable tail gas, the liquid phase enters the light component removal tower for rectification separation, the separated steam is mixed with the gas phase before entering the second gas-liquid separation device in the light component removal tower, and the separated liquid phase is treated by a reboiler and a subcooler at the bottom of the light component removal tower to obtain high-purity liquid carbon dioxide.
Preferably, the first gas-liquid separation device comprises a first condenser and a first gas-liquid separator, wherein the first condenser is connected with a steam outlet at the top of the heavy removal tower, and an inlet of the first gas-liquid separator is connected with an outlet of the first condenser; the second gas-liquid separation device comprises a second condenser and a second gas-liquid separator, the second condenser is connected with a gas phase outlet of the first gas-liquid separator, an inlet of the second gas-liquid separator is connected with an outlet of the second condenser, and a steam outlet at the top of the light component removal tower is communicated with an inlet of the second condenser. Through the two condensation and gas-liquid separation actions of the first gas-liquid separation device and the second gas-liquid separation device, the separation of the non-condensable tail gas can be more thorough, and the purity of the liquid carbon dioxide obtained at the bottom of the light component removal tower is greatly improved.
Preferably, the liquid phase outlet of the first gas-liquid separator is communicated with the heavy-removal tower to form reflux. After gas-liquid separation, the gas phase enters the next working procedure, and the liquid phase condensate flows back into the heavy-duty removal tower for circulating separation, so that the rectifying separation effect is ensured.
Preferably, the heat exchanger is a plate heat exchanger. The plate heat exchanger is adopted to make the waste liquid and the raw material gas exchange heat, and simultaneously gasify the waste liquid, so that the heat transfer coefficient is high and the heat transfer effect is good.
The invention also provides a method for treating the waste liquid of carbon dioxide rectification separation, which comprises the following steps:
the raw material gas is compressed and then is subjected to rectification separation, steam generated after separation is subjected to gas-liquid separation to obtain non-condensable tail gas, waste liquid generated after separation enters a heat exchanger to exchange heat with the raw material gas, the raw material gas after heat exchange enters a compression procedure, the waste liquid after heat exchange is gasified and enters a buffer tank to be mixed with the non-condensable tail gas, and when the mixed gas in the buffer tank reaches the emission standard, the buffer tank is emptied.
Preferably, the rectification separation step comprises separation by a heavy component removing tower and separation by a light component removing tower, wherein heavy component waste liquid is generated at the bottom of the tower after the separation by the heavy component removing tower, vapor generated at the top of the tower is subjected to first condensation and gas-liquid separation to obtain a gas phase and a liquid phase, the liquid phase flows back into the heavy component removing tower, the gas phase is subjected to second condensation and gas-liquid separation, the non-condensable tail gas and the liquid phase obtained at the moment are subjected to second condensation and gas-liquid separation, the liquid phase enters the light component removing tower again to be separated, liquid carbon dioxide is obtained at the bottom of the tower, and the gas phase discharged from the top of the tower is subjected to second condensation and gas-liquid separation in a gas-phase mixing cycle.
In summary, due to the adoption of the technical scheme, the beneficial effects of the invention are as follows:
1. according to the invention, the raw material gas exchanges heat with the heavy component waste liquid from the bottom of the heavy component removal tower, and the waste liquid absorbs a large amount of heat in the process of gasification and decompression in the heat exchanger, so that the raw material gas is cooled, the air inflow of the gas compressor can be increased by cooling the raw material gas, the processing capacity of the system in unit time is improved, the yield of the subsequent liquid carbon dioxide is increased, the production efficiency is improved, and the purpose of increasing the yield is achieved.
2. The invention is based on that the waste liquid has a large amount of cold energy, and the raw material gas exchanges heat with the heavy component waste liquid from the bottom of the heavy component removal tower, so that a large amount of heat is absorbed by the waste liquid in the process of gasification and decompression in the heat exchanger, and the cold energy of the waste liquid is reused, thereby achieving the effects of energy recovery and energy conservation.
3. Compared with the prior art, the treatment method of the heavy component waste liquid at the bottom of the heavy component removal tower is simpler and more convenient, greatly simplifies the waste liquid treatment process and equipment, and meets the environmental protection requirement.
Drawings
The invention will now be described by way of example and with reference to the accompanying drawings in which:
FIG. 1 is a schematic diagram of a waste liquid treatment apparatus according to the present invention.
Marked in the figure as: 10-gas compressor, 20-heavy-duty removal tower, 30-first gas-liquid separation device, 31-first condenser, 32-first gas-liquid separator, 40-second gas-liquid separation device, 41-second condenser, 42-second gas-liquid separator, 50-light-duty removal tower, 60-buffer tank, 70-reboiler, 80-subcooler, 90-heat exchanger.
Detailed Description
The technical solutions of the embodiments of the present invention will be clearly and completely described in the following in conjunction with the embodiments, and it is apparent that the described embodiments are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
Example 1
Referring to fig. 1, the present embodiment provides a device for treating waste liquid from rectification separation of carbon dioxide, comprising:
a gas compressor 10 for compressing the gas and then feeding the compressed gas to a subsequent rectification separation process;
the inlet of the heavy-removal tower 20 is connected with the gas compressor 10, steam is discharged from the top of the heavy-removal tower 20, a reboiler 70 is arranged at the bottom of the heavy-removal tower 20, liquid is partially gasified by the reboiler 70, and the residual liquid is discharged as heavy component waste liquid;
a first gas-liquid separation device 30, the inlet of which is connected with the steam outlet at the top of the heavy-removal tower 20;
a second gas-liquid separation device 40, the inlet of which is connected to the gas phase outlet of the first gas-liquid separation device 30; the first gas-liquid separation device 30 condenses and separates gas and liquid from the vapor discharged from the top of the heavy-removal tower 20, the separated liquid phase flows back into the heavy-removal tower 20, the gas phase enters the second gas-liquid separation device 40 to be condensed and separated again, the separated gas phase is non-condensable tail gas, the separated liquid phase enters the light-removal tower 50 to be rectified and separated, the gas phase separated by the light-removal tower 50 is mixed with the gas before entering the second gas-liquid separation device 40, and the second condensation and gas-liquid separation operation is circularly carried out, so that the separation is more thorough, the product purity is improved, and the high-purity liquid carbon dioxide can be obtained from the bottom of the light-removal tower 50;
the light component removing tower 50, the inlet of which is connected with the liquid phase outlet of the second gas-liquid separation device 40, the bottom liquid is gasified partially by the reboiler 70, and the rest liquid is passed through the cooler 80 to obtain liquid carbon dioxide;
the heat exchanger 90 is provided with a raw gas inlet, a raw gas outlet, a waste liquid inlet and a waste gas outlet, wherein the waste liquid inlet is connected with a waste liquid outlet at the bottom of the weight-removal tower 20, the raw gas outlet is connected with an air inlet of the gas compressor 10, raw gas enters the heat exchanger 90 to exchange heat with heavy component waste liquid from the weight-removal tower 20, and the waste liquid absorbs a large amount of heat in the process of gasification and decompression in the heat exchanger 90 so as to cool the raw gas, the cooled raw gas enters the gas compressor 10 again, the air inflow of the gas compressor 10 can be increased through cooling the raw gas, the treatment capacity of the system is improved, and the yield of the subsequent liquid carbon dioxide is increased; and
Buffer tank 60 is connected with the waste gas outlet of heat exchanger 90 and is connected with the gas phase outlet of second gas-liquid separation device 40, waste liquid is gasified after entering heat exchanger 90, is discharged from the waste gas outlet of heat exchanger 90 and enters buffer tank 60 to be mixed with non-condensable tail gas from the gas phase outlet of second gas-liquid separation device 40, and is emptied after reaching the standard.
Working principle:
the raw gas enters the heat exchanger 90 to exchange heat with heavy component waste liquid from the bottom of the heavy component removal tower 20, the waste liquid absorbs a large amount of heat in the process of gasification and decompression in the heat exchanger 90 so as to cool the raw gas, the cooled raw gas enters the gas compressor 10 again, the compressed raw gas enters the heavy component removal tower 20 to be rectified and separated, the separated steam is condensed by the first gas-liquid separation device 30 and separated into gas phase and liquid phase, the liquid phase condensate flows back into the heavy component removal tower 20, the heavy component waste liquid generated by separation is used for exchanging heat with the raw gas, the cold energy of the waste liquid is reused, and the air input of the gas compressor 10 can be increased by cooling the raw gas due to the fact that the waste liquid absorbs a large amount of heat in the heat exchanger 90, so that the yield of the subsequent liquid carbon dioxide is increased, and the purpose of energy conservation and yield increase is achieved.
The gas phase separated by the first gas-liquid separation device 30 enters the second gas-liquid separation device 40 to be condensed again and separated into gas and liquid, at this time, the separated gas phase is used as non-condensable tail gas, the liquid phase enters the light component removal tower 50 to be rectified and separated, the separated steam is mixed with the gas phase before entering the second gas-liquid separation device 40 in the light component removal tower 50, and the separated liquid phase is treated by the reboiler 70 and the subcooler 80 at the bottom of the light component removal tower 50 to obtain high-purity liquid carbon dioxide.
Example 2
Referring to fig. 1, on the basis of embodiment 1, the first gas-liquid separation device 30 includes a first condenser 31 and a first gas-liquid separator 32, the first condenser 31 is connected to a steam outlet at the top of the heavy-removal column 20, and an inlet of the first gas-liquid separator 32 is connected to an outlet of the first condenser 31; the second gas-liquid separation device 40 comprises a second condenser 41 and a second gas-liquid separator 42, the second condenser 41 is connected with the gas phase outlet of the first gas-liquid separator 32, the inlet of the second gas-liquid separator 42 is connected with the outlet of the second condenser 41, and the steam outlet at the top of the light component removal tower 50 is communicated with the inlet of the second condenser 41. Through the two condensation and gas-liquid separation actions of the first gas-liquid separation device 30 and the second gas-liquid separation device 40, the separation of the non-condensable tail gas can be more thorough, and the purity of the liquid carbon dioxide obtained at the bottom of the light component removal tower 50 can be greatly improved.
Example 3
Referring to fig. 1, on the basis of example 2, the liquid phase outlet of the first gas-liquid separator 32 communicates with the weight separator 20 to form a reflux. After gas-liquid separation, the gas phase enters the next working procedure, and the liquid phase condensate flows back into the heavy-duty removal tower 20 for circulating separation, so that the rectifying separation effect is ensured.
Example 4
Referring to fig. 1, in accordance with any of the embodiments, the heat exchanger 90 is a plate heat exchanger. The plate heat exchanger is adopted to make the waste liquid and the raw material gas exchange heat, and simultaneously gasify the waste liquid, so that the heat transfer coefficient is high and the heat transfer effect is good.
Example 5
The embodiment provides a method for treating waste liquid from carbon dioxide rectification separation, which comprises the following steps:
the raw material gas is compressed and then is subjected to rectification separation, steam generated after separation is subjected to gas-liquid separation to obtain non-condensable tail gas, waste liquid generated after separation enters a heat exchanger 90 to exchange heat with the raw material gas, the raw material gas after heat exchange enters a compression procedure, the waste liquid after heat exchange is gasified and enters a buffer tank 60 to be mixed with the non-condensable tail gas, and when the mixed gas in the buffer tank 60 reaches the emission standard, the mixed gas is discharged.
Preferably, the rectification separation step includes separation in a heavy component removal column 20 and separation in a light component removal column 50, wherein heavy component waste liquid is generated at the bottom of the column after separation in the heavy component removal column 20, vapor generated at the top of the column is subjected to first condensation and gas-liquid separation to obtain a gas phase and a liquid phase, the liquid phase flows back into the heavy component removal column 20, the gas phase is subjected to second condensation and gas-liquid separation, the obtained non-condensable tail gas and the liquid phase are subjected to second condensation and gas-liquid separation, the liquid phase is subjected to separation in the light component removal column 50, liquid carbon dioxide is obtained at the bottom of the column, and the gas phase is discharged from the top of the column and is subjected to second condensation and gas-liquid separation in a gas phase mixing cycle from the heavy component removal column 20.
Experimental example
Taking 7 tons of liquid carbon dioxide produced in each hour by a double rectifying tower as an example, raw material gas CO 2 The purity is 88.3%, the inlet pressure of the raw material gas is 20KPa, the temperature is 30 ℃, the pressure is increased to 2.45MPa after passing through a compressor, then the raw material gas is subjected to rectification separation by a light component removal tower and a heavy component removal tower, the waste liquid with the temperature of minus 10 ℃ is discharged from the bottom of the heavy component removal tower, the flow is 75Kg/h, and the non-condensable tail gas is 665Nm discharged from the top of the light component removal tower 3 And/h. Waste liquid pipeThe plate-passing type heat exchanger exchanges heat with the raw material gas before entering the compressor, so that the temperature of the raw material gas is reduced to 26 ℃. This allows the compressor to run at 20KPa for 306m more per hour 3 The final yield of feed gas can be increased by 0.088 tons per hour (1.26% of feed gas). The waste liquid after heat exchange is gasified, and is directly discharged after being mixed with non-condensable tail gas discharged from the top of the light component removal tower in a buffer tank, and the content and the discharge requirements of each component of the discharged gas are shown in the following table.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present invention, and are not limiting; although the invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced with equivalents; such modifications and substitutions do not depart from the spirit of the invention, and are intended to be included within the scope of the appended claims and description.
Claims (3)
1. A carbon dioxide rectifying and separating waste liquid treatment device, characterized by comprising:
a gas compressor;
the inlet of the heavy-removal tower is connected with the gas compressor; a reboiler is arranged at the bottom of the heavy-component removal tower, the liquid is gasified by the reboiler part, and the residual liquid is discharged as heavy-component waste liquid;
the inlet of the first gas-liquid separation device is connected with a steam outlet at the top of the heavy-removal tower;
the inlet of the second gas-liquid separation device is connected with the gas phase outlet of the first gas-liquid separation device;
the inlet of the light component removing tower is connected with the liquid phase outlet of the second gas-liquid separation device;
the heat exchanger is provided with a raw material gas inlet, a raw material gas outlet, a waste liquid inlet and a waste gas outlet, wherein the waste liquid inlet is connected with a waste liquid outlet at the bottom of the heavy-removal tower, and the raw material gas outlet is connected with a gas inlet of the gas compressor;
the buffer tank is connected with the waste gas outlet of the heat exchanger and is also connected with the gas phase outlet of the second gas-liquid separation device;
the first gas-liquid separation device comprises a first condenser and a first gas-liquid separator, the first condenser is connected with a steam outlet at the top of the heavy removal tower, and an inlet of the first gas-liquid separator is connected with an outlet of the first condenser; the second gas-liquid separation device comprises a second condenser and a second gas-liquid separator, the second condenser is connected with a gas phase outlet of the first gas-liquid separator, an inlet of the second gas-liquid separator is connected with an outlet of the second condenser, and a steam outlet at the top of the light component removal tower is communicated with an inlet of the second condenser;
the liquid phase outlet of the first gas-liquid separator is communicated with the weight removing tower to form reflux;
the heat exchanger is a plate heat exchanger.
2. A method for treating waste liquid of carbon dioxide rectification separation applied to a device for treating waste liquid of carbon dioxide rectification separation as claimed in claim 1, characterized by comprising the steps of:
the raw material gas is compressed and then is subjected to rectification separation, steam generated after separation is subjected to gas-liquid separation to obtain non-condensable tail gas, waste liquid generated after separation is subjected to heat exchange with the raw material gas, the raw material gas subjected to heat exchange enters a compression procedure, the waste liquid subjected to heat exchange is gasified and enters a buffer tank to be mixed with the non-condensable tail gas, and when the mixed gas in the buffer tank reaches the emission standard, the buffer tank is emptied.
3. The method according to claim 2, wherein the rectifying and separating step comprises a separation by a weight removal column and a separation by a weight removal column, wherein the waste liquid is produced at the bottom of the separation by the weight removal column, the vapor produced at the top of the column is subjected to first condensation and gas-liquid separation to obtain a gas phase and a liquid phase, the liquid phase is returned to the weight removal column, the gas phase is subjected to second condensation and gas-liquid separation, the obtained non-condensable tail gas and liquid phase are subjected to second condensation and gas-liquid separation, the liquid phase is subjected to separation by the weight removal column, the liquid carbon dioxide is obtained at the bottom of the column, and the gas phase discharged from the top of the column is subjected to second condensation and gas-liquid separation by a gas phase mixing cycle.
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