CN111256432A - Device and method for treating carbon dioxide rectification separation waste liquid - Google Patents
Device and method for treating carbon dioxide rectification separation waste liquid Download PDFInfo
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- CN111256432A CN111256432A CN202010170999.XA CN202010170999A CN111256432A CN 111256432 A CN111256432 A CN 111256432A CN 202010170999 A CN202010170999 A CN 202010170999A CN 111256432 A CN111256432 A CN 111256432A
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- 239000007788 liquid Substances 0.000 title claims abstract description 192
- 238000000926 separation method Methods 0.000 title claims abstract description 124
- 239000002699 waste material Substances 0.000 title claims abstract description 79
- 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 38
- 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 164
- 239000002994 raw material Substances 0.000 claims abstract description 42
- 239000012071 phase Substances 0.000 claims abstract description 39
- 239000007791 liquid phase Substances 0.000 claims abstract description 33
- 239000002912 waste gas Substances 0.000 claims abstract description 9
- 238000009833 condensation Methods 0.000 claims description 16
- 230000005494 condensation Effects 0.000 claims description 15
- 238000007906 compression Methods 0.000 claims description 4
- 238000010992 reflux Methods 0.000 claims description 3
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- 230000000694 effects Effects 0.000 description 7
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- 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
- 239000007792 gaseous phase Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 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
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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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- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention discloses a carbon dioxide rectification separation waste liquid treatment device, which relates to the technical field of carbon dioxide rectification separation and comprises the following components: a gas compressor; the inlet of the heavy component removing tower is connected with a gas compressor; the inlet of the first gas-liquid separation device is connected with the steam outlet at the top of the de-heavy 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 removal 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, the waste liquid inlet is connected with the waste liquid outlet at the bottom of the de-heavy 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 simultaneously connected with the gas phase outlet of the second gas-liquid separation device. The invention exchanges heat between the feed gas and 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 system yield 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 the carbon dioxide rectification separation.
Background
With the rapid development of the industry, CO, a major greenhouse gas2The annual emission amount is more and more, which has to worry, meanwhile, 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 the carbon resource can be comprehensively utilized, and the environmental pollution caused by industrial waste gas emission can be treated.
At present, the industrial production of carbon dioxide mainly utilizes industrial carbon-containing waste gas (CO)2Content > 80%) of the extract. The exhaust gas contains CO2In addition, it may also contain H2S、COS、C2H4、C2H6、C3H6、C6H6、CH3OH and the like. There are generally two methods for separating these impurities, one is to remove H first by physical or chemical adsorption2S, then converting the organic hydrocarbons into H by oxidative combustion2O、CO2Wherein, the adsorbent is used for a plurality of times and then used as dangerous solid waste to be buried, and the catalyst for oxidation and dealkylation is also refined and buried after being used for a long time. And secondly, by a rectification process, the components are discharged from the bottom of the de-heavy tower by utilizing the difference of relative volatility, and are collected and then are treated in a centralized way.
However, the carbon dioxide rectification separation process generates a large amount of waste liquid, the waste liquid is discharged from the bottom of the de-heavy tower, the temperature is lower than-12 ℃, and the content of sulfur and benzene in the waste liquid exceeds 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 to: the utility model provides a carbon dioxide rectification separation waste liquid processing apparatus and method, through with the feed gas with come from the heavy ends waste liquid heat transfer of heavy ends bottom, make the cold energy recycle of waste liquid, reach energy recovery, the effect of energy saving, thereby the waste liquid gasifies in the heat exchanger, the process of decompression absorbs a large amount of heats makes the feed gas cooling simultaneously, the cooling of feed gas can make the air input of gas compressor increase, thereby the handling capacity of system has been improved, the output of follow-up liquid carbon dioxide has been increased, reach the purpose of raising the production.
The technical scheme adopted by the invention is as follows:
in order to achieve the above object, the present invention provides a carbon dioxide rectification separation waste liquid treatment apparatus, comprising:
the gas compressor is used for compressing the gas and then sending the compressed gas to the subsequent rectification separation process;
the inlet of the heavy component removal tower is connected with a gas compressor, steam is discharged from the top of the heavy component removal tower, a reboiler is arranged at the bottom of the heavy component removal tower, liquid is partially 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 the steam outlet at the top of the de-heavy 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 carries out condensation and gas-liquid separation on steam discharged from the top of the heavy component removal tower, the separated liquid phase flows back into the heavy component removal tower, the gas phase enters the second gas-liquid separation device for condensation and gas-liquid separation again, the separated gas phase is non-condensable tail gas at the moment, the separated liquid phase enters the light component removal tower for rectification and separation, the gas phase separated by the light component removal tower is mixed with gas before entering the second gas-liquid separation device, and secondary condensation and gas-liquid separation operation is carried out in a circulating mode, so that separation is more thorough, the product purity is improved, and high-purity liquid carbon dioxide can be obtained from the bottom of the light component removal tower;
the inlet of the light component removal tower is connected with the liquid phase outlet of the second gas-liquid separation device, the liquid at the bottom of the tower is partially gasified by a reboiler, and the rest liquid is cooled by 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, the waste liquid inlet is connected with the waste liquid outlet at the bottom of the de-weighting tower, the raw material gas outlet is connected with a gas inlet of the gas compressor, the raw material gas enters the heat exchanger to exchange heat with the heavy component waste liquid from the de-weighting tower, the waste liquid absorbs a large amount of heat in the processes of gasification and pressure reduction in the heat exchanger so as to cool the raw material gas, the cooled raw material gas enters the gas compressor again, the air input of the gas compressor can be increased through cooling the raw material gas, the treatment capacity of the system is improved, and; and
the buffer tank is connected with the waste gas outlet of the heat exchanger and is simultaneously connected with the gas phase outlet of the second gas-liquid separation device, waste liquid is gasified after entering the heat exchanger, and is discharged from the waste gas outlet of the heat exchanger to enter the buffer tank to be mixed with non-condensable tail gas from the gas phase outlet of the second gas-liquid separation device, and the waste liquid is emptied after reaching the standard.
The working principle is as follows:
the method comprises the following steps that raw material gas enters a heat exchanger to exchange heat with heavy component waste liquid from the bottom of a heavy component removal tower, the waste liquid absorbs a large amount of heat in the process of gasification and pressure reduction in the heat exchanger so as to cool the raw material gas, the cooled raw material gas enters a gas compressor again, the compressed raw material gas enters the heavy component removal tower to be rectified and separated, separated steam is condensed by a first gas-liquid separation device and is separated from gas and liquid to obtain gas phase and liquid phase, liquid phase condensate flows back into the heavy component removal tower, the heavy component waste liquid generated by separation is used for exchanging heat with the raw material gas, cold energy of the waste liquid is reused, the waste liquid absorbs a large amount of heat in the process of gasification and pressure reduction in the heat exchanger so as to cool the raw material gas, the air input of the gas compressor can be increased through cooling the raw material gas.
And the gas phase obtained by separation of the first gas-liquid separation device enters a second gas-liquid separation device for secondary condensation and gas-liquid separation, the gas phase obtained by separation is used as non-condensable tail gas, the liquid phase enters a light component removal tower for rectification and 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, the first condenser is connected with a steam outlet at the top of the de-heavy 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 twice condensation and gas-liquid separation effects of the first gas-liquid separation device and the second gas-liquid separation device, the non-condensable tail gas can be separated more thoroughly, 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 de-heavy column to form reflux. After gas-liquid separation, the gas phase enters the next working procedure, and the liquid phase condensate flows back to the de-heavy tower for circular separation, so that the effect of rectification separation is ensured.
Preferably, the heat exchanger is a plate heat exchanger. The plate heat exchanger is adopted to exchange heat between the waste liquid and the raw material gas, 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 carbon dioxide rectification separation waste liquid, which comprises the following steps:
the feed gas is subjected to rectification separation after compression, non-condensable tail gas is obtained through gas-liquid separation of steam generated after separation, waste liquid generated after separation enters a heat exchanger to exchange heat with the feed gas, the feed gas after heat exchange enters a compression process, the waste liquid after heat exchange is gasified and enters a buffer tank to be mixed with the non-condensable tail gas, and when mixed gas in the buffer tank reaches a discharge standard, the mixed gas is discharged.
Preferably, the rectification separation step comprises heavy component removal tower separation and light component removal tower separation, heavy component waste liquid is generated at the bottom of the heavy component removal tower after the heavy component removal tower separation, 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 to the heavy component removal tower, the gas phase is subjected to second condensation and gas-liquid separation, non-condensable tail gas and the liquid phase are obtained at the moment, liquid carbon dioxide is obtained at the bottom of the light component removal tower after the liquid phase enters the light component removal tower for separation, and gas phase discharged from the top of the tower is mixed with gas phase from the heavy component removal tower for circulation to perform second.
In summary, due to the adoption of the technical scheme, the invention has the beneficial effects that:
1. the invention exchanges heat with the heavy component waste liquid from the bottom of the heavy component removal tower through the feed gas, the waste liquid absorbs a large amount of heat in the processes of gasification and pressure reduction in the heat exchanger so as to cool the feed gas, and the cooling of the feed gas can increase the air input of the gas compressor, thereby improving the treatment capacity of the system in unit time, increasing the output of subsequent liquid carbon dioxide, improving the production efficiency and achieving the purpose of increasing the yield.
2. The invention is based on the fact that the waste liquid has a large amount of cold energy, the raw gas and the heavy component waste liquid from the bottom of the heavy component removal tower exchange heat, the waste liquid absorbs a large amount of heat in the processes of gasification and pressure reduction in the heat exchanger, and the cold energy of the waste liquid is reused, so that the effects of energy recovery and energy saving are achieved.
3. Compared with the prior art, the method for treating 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 requirement of environmental protection.
Drawings
The invention will now be described, by way of example, with reference to the accompanying drawings, in which:
FIG. 1 is a schematic view showing the structure of a waste liquid treatment apparatus according to the present invention.
Labeled as: 10-a gas compressor, 20-a heavy component removal tower, 30-a first gas-liquid separation device, 31-a first condenser, 32-a first gas-liquid separator, 40-a second gas-liquid separation device, 41-a second condenser, 42-a second gas-liquid separator, 50-a light component removal tower, 60-a buffer tank, 70-a reboiler, 80-a subcooler and 90-a heat exchanger.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the following embodiments, and it should be understood that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
Referring to fig. 1, the present embodiment provides a carbon dioxide rectification separation waste liquid treatment device, including:
the gas compressor 10 is used for compressing the gas and then sending the gas into a subsequent rectification separation process;
a heavy component removal tower 20, the inlet of which is connected with the gas compressor 10, the top of the heavy component removal tower 20 discharges steam, the bottom of the heavy component removal tower 20 is provided with a reboiler 70, 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 de-heavy tower 20;
a second gas-liquid separation device 40, an inlet of which is connected with 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 steam discharged from the top of the heavy component removal tower 20, the separated liquid phase flows back into the heavy component removal tower 20, the gas phase enters the second gas-liquid separation device 40 for condensation and gas-liquid separation again, the separated gas phase is non-condensable tail gas at the moment, the separated liquid phase enters the light component removal tower 50 for rectification and separation, the gas phase separated by the light component 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 performed, so that the separation is more thorough, the product purity is favorably improved, and high-purity liquid carbon dioxide can be obtained from the bottom of the light component removal tower 50;
a light component removal tower 50, the inlet of which is connected with the liquid phase outlet of the second gas-liquid separation device 40, the liquid at the bottom of the tower is partially gasified by a reboiler 70, and the rest liquid is cooled by a cooler 80 to obtain liquid carbon dioxide;
the heat exchanger 90 is provided with a raw material gas inlet, a raw material gas outlet, a waste liquid inlet and a waste gas outlet, the waste liquid inlet is connected with the waste liquid outlet at the bottom of the de-weighting tower 20, the raw material gas outlet is connected with the gas inlet of the gas compressor 10, the raw material gas enters the heat exchanger 90 to exchange heat with the heavy component waste liquid from the de-weighting tower 20, the waste liquid absorbs a large amount of heat in the processes of gasification and pressure reduction in the heat exchanger 90 so as to cool the raw material gas, the cooled raw material gas enters the gas compressor 10 again, the air input of the gas compressor 10 can be increased through cooling the raw material gas, the treatment capacity of the system is improved, and; and
The working principle is as follows:
the raw material gas enters the heat exchanger 90 to exchange heat with the 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 processes of gasification and pressure reduction in the heat exchanger 90 so as to cool the raw material gas, the cooled raw material gas enters the gas compressor 10 again, the cooled raw material gas enters the heavy component removal tower 20 after being compressed and then is rectified and separated, the separated steam is condensed and separated by the first gas-liquid separation device 30 to obtain a gas phase and a 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 material gas, and the cold energy of, because the waste liquid absorbs a large amount of heat in the process of gasification and pressure reduction in the heat exchanger 90, the temperature of the raw material gas is reduced, the air input of the gas compressor 10 can be increased by cooling the raw gas, and the treatment capacity of the system is improved, so that the output of subsequent liquid carbon dioxide is increased, and the purposes of saving energy and increasing yield are achieved.
The gas phase obtained by the separation of the first gas-liquid separation device 30 enters the second gas-liquid separation device 40 for re-condensation and gas-liquid separation, the gas phase obtained by the separation is used as non-condensable tail gas, the liquid phase enters the lightness-removing tower 50 for rectification and separation, in the lightness-removing tower 50, the separated steam is mixed with the gas phase before entering the second gas-liquid separation device 40, and the separated liquid phase is treated by the reboiler 70 and the subcooler 80 at the bottom of the lightness-removing 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 comprises a first condenser 31 and a first gas-liquid separator 32, the first condenser 31 is connected with a steam outlet at the top of the de-heavy tower 20, and an inlet of the first gas-liquid separator 32 is connected with 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 lightness-removing column 50 is communicated with the inlet of the second condenser 41. Through the twice condensation and gas-liquid separation actions of the first gas-liquid separation device 30 and the second gas-liquid separation device 40, the non-condensable tail gas can be separated more thoroughly, and the purity of the liquid carbon dioxide obtained at the bottom of the light component removal tower 50 is greatly improved.
Example 3
Referring to fig. 1, in example 2, the liquid phase outlet of the first gas-liquid separator 32 is communicated with the de-heavy column 20 to form a reflux stream. After gas-liquid separation, the gas phase enters the next process, and the liquid phase condensate flows back to the de-heavy tower 20 for circular separation, so that the rectification separation effect is ensured.
Example 4
Referring to fig. 1, in any embodiment, the heat exchanger 90 is a plate heat exchanger. The plate heat exchanger is adopted to exchange heat between the waste liquid and the raw material gas, 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 generated in carbon dioxide rectification separation, which comprises the following steps:
the feed gas is rectified and separated after being compressed, non-condensable tail gas is obtained by gas-liquid separation of steam generated after separation, waste liquid generated after separation enters a heat exchanger 90 to exchange heat with the feed gas, the feed gas after heat exchange enters a compression process, 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 discharge standard, the mixed gas is discharged.
Preferably, the rectification separation step comprises separation in a heavy component removal tower 20 and separation in a light component removal tower 50, heavy component waste liquid is generated at the bottom of the heavy component removal tower 20 after the separation, 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 to the heavy component removal tower 20, the gas phase is subjected to second condensation and gas-liquid separation, non-condensable tail gas and a liquid phase are obtained at the moment, the liquid phase is further subjected to separation in the light component removal tower 50, liquid carbon dioxide is obtained at the bottom of the tower, and the gas phase discharged at the top of the tower is mixed with the gas phase from the heavy component removal tower 20 and circulated to.
Examples of the experiments
Taking the example of double rectification towers producing 7 tons of liquid carbon dioxide per hour as raw material gas CO2The purity is 88.3%, the pressure of the raw material gas inlet is 20KPa, the temperature is 30 ℃, the pressure is increased to 2.45MPa after passing through a compressor, then the raw material gas is rectified and separated by a light component removal tower and a heavy component removal tower, 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 665Nm is discharged from the top of the light component removal tower3H is used as the reference value. The waste liquid exchanges heat with the raw material gas before entering the compressor through the plate heat exchanger, so that the temperature of the raw material gas is reduced to 26 ℃. This can make the compressor beat 306m more per hour at 20KPa3The final yield of the raw material gas can be increased by 0.088 tons (1.26 percent of the raw material gas) per hour. 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 requirement of each component of the discharged gas are shown in the following table.
Finally, it should be noted that: the above examples are only intended to illustrate the technical solution of the present invention, but not to limit it; although the present 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 solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; these modifications and substitutions do not cause the essence of the corresponding technical solution to depart from the scope of the technical solution of the embodiments of the present invention, and are intended to be covered by the claims and the specification of the present invention.
Claims (6)
1. A carbon dioxide rectification separation waste liquid treatment device is characterized by comprising:
a gas compressor;
the inlet of the heavy component removing tower is connected with a gas compressor;
the inlet of the first gas-liquid separation device is connected with the steam outlet at the top of the de-heavy 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 removal 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, the waste liquid inlet is connected with the waste liquid outlet at the bottom of the de-heavy tower, and the raw material gas outlet is connected with a gas inlet of the gas compressor; and
and the buffer tank is connected with the waste gas outlet of the heat exchanger and is simultaneously connected with the gas phase outlet of the second gas-liquid separation device.
2. The device for treating the waste liquid generated in the rectification separation of the carbon dioxide as claimed in claim 1, wherein 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 de-heavy 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.
3. The apparatus as claimed in claim 2, wherein the liquid phase outlet of the first gas-liquid separator is connected to the de-heavy column to form a reflux.
4. The device for treating the carbon dioxide rectification separation waste liquid according to any one of claims 1 to 3, wherein the heat exchanger is a plate heat exchanger.
5. A method for treating waste liquid generated in the process of rectifying and separating carbon dioxide is characterized by comprising the following steps:
the feed gas is rectified and separated after being compressed, non-condensable tail gas is obtained through gas-liquid separation of steam generated after separation, waste liquid generated after separation exchanges heat with the feed gas, the feed gas after heat exchange enters a compression process, the waste liquid after heat exchange is gasified and enters a buffer tank to be mixed with the non-condensable tail gas, and when mixed gas in the buffer tank reaches a discharge standard, the mixed gas is discharged.
6. The method for treating the waste liquid generated in the rectification separation of the carbon dioxide as claimed in claim 5, wherein the rectification separation step comprises heavy component removal column separation and light component removal column separation, waste liquid is generated at the bottom of the heavy component removal column separation, 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 to the heavy component removal column, the gas phase is subjected to second condensation and gas-liquid separation to obtain non-condensable tail gas and a liquid phase, the liquid phase is subjected to separation in the light component removal column, liquid carbon dioxide is obtained at the bottom of the column, and the gas phase discharged at the top of the column is mixed with the gas phase from the heavy component removal column to be circulated for second condensation and gas.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114963691A (en) * | 2022-05-31 | 2022-08-30 | 山东石油化工学院 | Low pressure CO 2 Low-temperature gas separation method and device |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101289957A (en) * | 2007-07-12 | 2008-10-22 | 李钢坤 | Follow-up hydrogen making engine fuel system and its device |
| US20100101273A1 (en) * | 2008-10-27 | 2010-04-29 | Sechrist Paul A | Heat Pump for High Purity Bottom Product |
| CN104654739A (en) * | 2015-02-02 | 2015-05-27 | 河南心连心深冷能源股份有限公司 | Device and method for preparing food-grade liquid carbon dioxide by rectification and purification with double towers |
| CN204513904U (en) * | 2015-02-02 | 2015-07-29 | 河南心连心深冷能源股份有限公司 | Utilize two-tower rectification to purify and produce the device of food-class liquid CO 2 |
| US20170267615A1 (en) * | 2014-06-05 | 2017-09-21 | Shanghai Wuzheng Engineering Technology Co., Ltd | Method and device system for producing dimethyl oxalate through midhigh and high-pressure carbonylation of industrial synthesis gas and producing ethylene glycol through dimethyl oxalate hydrogenation |
| CN109084527A (en) * | 2018-09-20 | 2018-12-25 | 中科瑞奥能源科技股份有限公司 | Laughing gas rectification and purification device and laughing gas rectificating method |
| CN110841453A (en) * | 2019-12-17 | 2020-02-28 | 金昌隆博气体有限责任公司 | Novel high-purity acetylene purification production system and process flow thereof |
| CN211782272U (en) * | 2020-03-12 | 2020-10-27 | 金昌隆博气体有限责任公司 | Carbon dioxide rectification separation waste liquid treatment device |
-
2020
- 2020-03-12 CN CN202010170999.XA patent/CN111256432B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101289957A (en) * | 2007-07-12 | 2008-10-22 | 李钢坤 | Follow-up hydrogen making engine fuel system and its device |
| US20100101273A1 (en) * | 2008-10-27 | 2010-04-29 | Sechrist Paul A | Heat Pump for High Purity Bottom Product |
| US20170267615A1 (en) * | 2014-06-05 | 2017-09-21 | Shanghai Wuzheng Engineering Technology Co., Ltd | Method and device system for producing dimethyl oxalate through midhigh and high-pressure carbonylation of industrial synthesis gas and producing ethylene glycol through dimethyl oxalate hydrogenation |
| CN104654739A (en) * | 2015-02-02 | 2015-05-27 | 河南心连心深冷能源股份有限公司 | Device and method for preparing food-grade liquid carbon dioxide by rectification and purification with double towers |
| CN204513904U (en) * | 2015-02-02 | 2015-07-29 | 河南心连心深冷能源股份有限公司 | Utilize two-tower rectification to purify and produce the device of food-class liquid CO 2 |
| CN109084527A (en) * | 2018-09-20 | 2018-12-25 | 中科瑞奥能源科技股份有限公司 | Laughing gas rectification and purification device and laughing gas rectificating method |
| CN110841453A (en) * | 2019-12-17 | 2020-02-28 | 金昌隆博气体有限责任公司 | Novel high-purity acetylene purification production system and process flow thereof |
| CN211782272U (en) * | 2020-03-12 | 2020-10-27 | 金昌隆博气体有限责任公司 | Carbon dioxide rectification separation waste liquid treatment device |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114963691A (en) * | 2022-05-31 | 2022-08-30 | 山东石油化工学院 | Low pressure CO 2 Low-temperature gas separation method and device |
| CN114963691B (en) * | 2022-05-31 | 2023-12-26 | 山东石油化工学院 | Low pressure CO 2 Gas low-temperature separation method and device |
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