CN117928172A - High-purity liquid CO utilizing LNG cold energy2Production method and system - Google Patents
High-purity liquid CO utilizing LNG cold energy2Production method and system Download PDFInfo
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- CN117928172A CN117928172A CN202410007083.0A CN202410007083A CN117928172A CN 117928172 A CN117928172 A CN 117928172A CN 202410007083 A CN202410007083 A CN 202410007083A CN 117928172 A CN117928172 A CN 117928172A
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- heat exchanger
- gas
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- liquid
- pressure
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- 239000007788 liquid Substances 0.000 title claims abstract description 108
- 238000000034 method Methods 0.000 title abstract description 43
- 238000005057 refrigeration Methods 0.000 claims abstract description 40
- 238000000746 purification Methods 0.000 claims abstract description 32
- 238000010248 power generation Methods 0.000 claims abstract description 24
- 239000002994 raw material Substances 0.000 claims abstract description 16
- 238000007906 compression Methods 0.000 claims abstract description 12
- 230000006835 compression Effects 0.000 claims abstract description 10
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 165
- 239000003949 liquefied natural gas Substances 0.000 claims description 103
- 239000001569 carbon dioxide Substances 0.000 claims description 79
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 79
- 239000007789 gas Substances 0.000 claims description 61
- 238000004519 manufacturing process Methods 0.000 claims description 28
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 16
- 238000001816 cooling Methods 0.000 claims description 14
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 12
- 238000003860 storage Methods 0.000 claims description 11
- 239000007791 liquid phase Substances 0.000 claims description 8
- 239000012071 phase Substances 0.000 claims description 8
- 239000001294 propane Substances 0.000 claims description 8
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 6
- 239000005977 Ethylene Substances 0.000 claims description 6
- 239000000498 cooling water Substances 0.000 claims description 4
- 230000008569 process Effects 0.000 abstract description 28
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 238000006243 chemical reaction Methods 0.000 abstract description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 18
- 239000000047 product Substances 0.000 description 12
- 239000012535 impurity Substances 0.000 description 9
- 239000000203 mixture Substances 0.000 description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- 229910052799 carbon Inorganic materials 0.000 description 7
- 235000011089 carbon dioxide Nutrition 0.000 description 7
- 239000003345 natural gas Substances 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 238000002309 gasification Methods 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 230000008901 benefit Effects 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 5
- 239000001257 hydrogen Substances 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 230000005611 electricity Effects 0.000 description 4
- 238000003723 Smelting Methods 0.000 description 3
- 239000012084 conversion product Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000012263 liquid product Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000000704 physical effect Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 238000004378 air conditioning Methods 0.000 description 1
- -1 alcohol amine Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000002778 food additive Substances 0.000 description 1
- 235000013373 food additive Nutrition 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000002427 irreversible effect Effects 0.000 description 1
- 239000001095 magnesium carbonate Substances 0.000 description 1
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 description 1
- 229910000021 magnesium carbonate Inorganic materials 0.000 description 1
- 235000014380 magnesium carbonate Nutrition 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 201000009240 nasopharyngitis Diseases 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
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- 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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- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0027—Oxides of carbon, e.g. CO2
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- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/005—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by expansion of a gaseous refrigerant stream with extraction of work
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- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
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- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
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- 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
- F25J3/0204—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 feed stream
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- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
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- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
- F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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- F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
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- F25J2215/80—Carbon dioxide
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- F25J2220/80—Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
- F25J2220/82—Separating low boiling, i.e. more volatile components, e.g. He, H2, CO, Air gases, CH4
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- F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
- F25J2260/10—Integration in a gas transmission system at a pressure reduction, e.g. "let down" station
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- F25J2270/00—Refrigeration techniques used
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
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Abstract
The invention belongs to the technical field of direct utilization of LNG cold energy, and particularly relates to a method and a system for producing high-purity liquid CO 2 by utilizing LNG cold energy. The system provided by the invention at least comprises a CO 2 pressure treatment subsystem, a Rankine cycle subsystem and a rectification purification subsystem, wherein the CO 2 pressure treatment subsystem exchanges heat with working medium of the Rankine cycle subsystem through CO 2 gas outlet so as to provide energy required by working medium power generation and work application, and the rectification purification subsystem purifies the exchanged CO 2 gas outlet. The invention converts the pressure energy of partial raw material gas into electric energy by a split expansion mode aiming at the high-pressure CO 2 raw material gas which is conveyed by the pipe, thereby increasing the energy conversion efficiency of the process; aiming at the CO 2 feed gas with lower pressure which is conveyed by the pipe, the pressure of part of the feed gas is increased by a split-flow compression mode, so that the purpose of increasing the liquefaction amount of CO 2 is achieved. And a rectification purification subsystem constructs refrigeration cycle between the condenser and the reboiler, and the refrigeration cycle utilizes LNG cold energy, so that refrigeration energy consumption is greatly reduced.
Description
Technical Field
The invention belongs to the technical field of direct utilization of LNG cold energy, and particularly relates to a method and a system for producing high-purity liquid CO 2 by utilizing LNG cold energy.
Background
Common cold energy utilization technologies for Liquefied Natural Gas (LNG) include power generation using LNG cold energy, air separation, liquid CO 2 or dry ice production, and the like. The cold energy power generation technology plays an important role as one of the main modes of LNG cold energy utilization.
The basic principle of power generation by utilizing LNG cold energy is generally that LNG is taken as a low-temperature cold source in a low-temperature power circulation process, and mechanical work generated by the low-temperature power circulation is utilized to drive a generator set to generate electric power.
The technical means is utilized to recycle the discharged CO 2 gas and fully utilize the waste heat resources carried by the CO 2 gas, so that the method has environmental protection significance for reducing the greenhouse effect and can cause the wasted waste heat resources to generate economic value.
The Chinese patent with the application number 201710658357.2 provides a carbon dioxide liquefying device, which aims at carbon dioxide coming from a flue gas carbon capturing system, is compressed to a supercritical state after impurities are removed, and utilizes throttling expansion to realize self liquefaction. The difference with the patent lies in that LNG cold energy is not utilized, the impurity removal part is simpler, the purity of product liquid is lower, and a great deal of work can be consumed when carbon dioxide is compressed to a supercritical state.
The chinese patent application No. 202310357469.X proposes a device for pressurizing and liquefying carbon dioxide by using LNG cold energy, which is different from the present patent in that no liquid-state oxidation and purification device is provided, and the cold energy conversion product is single and only one liquid carbon dioxide is provided.
The chinese patent of application number 201910049759.1 proposes a device for purifying carbon dioxide by liquefaction, which is different from the present patent in that it does not utilize LNG cold energy, has no output of work amount, and the purifying part is more complex.
In chinese patent No. 201910342318.0, a power generation system using carbon dioxide as a rankine cycle medium is proposed, in which LNG cold energy is recycled and a heat source of a first quality is used, but the system does not generate liquid carbon dioxide.
The application number is 202310563543.3, and an LNG cold energy utilization system integrating energy storage, carbon capture, air conditioning and the like is provided, and through combined application of the systems, the problems of insufficient LNG cold energy utilization and reality matching degree are scientifically solved, but the system is not provided with a liquid carbon dioxide purification system, and the produced liquid product can be industrially utilized only through purification.
The China patent with the application number 202220930402.1 proposes a carbon dioxide capturing and transferring device for a gas turbine set. The difference with the patent is that the produced liquid carbon dioxide is not purified, and the cold energy conversion product is single and has no output of work.
The China patent with the application number 202120785147.1 provides a carbon dioxide liquefying and purifying device utilizing LNG cold energy. The difference with the patent lies in that the cold energy conversion product is single, the output of no work amount is not good, and the output of liquid products can not be well regulated.
The patent with the application number 202211285506.2 discloses a direct air carbon dioxide capturing and utilizing system and a method for utilizing LNG cold energy, wherein the system comprises an LNG gasification cold release device, an air carbon dioxide capturing device and a carbon dioxide utilizing device. However, the process has single cold energy utilization product, no electric energy generation and unadjustable liquid carbon dioxide yield.
Patent number 201510339362.8 discloses a method for capturing carbon dioxide in ore smelting waste gas by utilizing LNG cold energy, belongs to the field of environmental protection, and particularly relates to a method for capturing carbon dioxide in waste gas generated by ore smelting by utilizing LNG cold energy. The invention can intensively collect carbon dioxide discharged by an unorganization, and greatly reduces carbon discharge in the smelting process of magnesite. And two-stage Rankine cycle power generation is combined, so that temperature opposite and cascade utilization are realized. However, the process does not purify the liquefied carbon dioxide and cannot be used in industrial production.
The patent application number 202210978747.9 discloses a high-efficiency integrated system and method for realizing LNG gasification export, natural gas reforming hydrogen production, hydrogen liquefaction and CO 2 liquefaction recovery through comprehensive optimized utilization of LNG cold energy in an LNG receiving station. The difference from this patent is that the ratio of liquid carbon dioxide production to power generation cannot be adjusted without the output of electrical energy.
Patent application number 202123015473.3 discloses a marine CO 2 liquefaction collection system using LNG cold energy, comprising a liquefaction processing unit, a collection and discharge unit and a diffusion unit. The difference with this patent lies in the difference that is suitable for the scene, and this patent is applicable to the inside cold energy utilization part of LNG receiving station, and the output of this patent no electric energy, the output of the regulation liquid carbon dioxide that can not be fine.
The patent number 202120613476.8 discloses a system for preparing dry ice by utilizing LNG cold energy, which comprises an LNG storage tank, a liquid carbon dioxide storage tank, a first heat exchanger, an ice drier and a compressor, wherein the LNG storage tank is used for providing liquefied natural gas, and the system is used for preparing dry ice, so that the carbon dioxide loss and the production electricity consumption are effectively reduced, and obvious environmental benefit and economic benefit are realized. However, the cold energy utilization product of the process is single, the product is dry ice, and no electric energy and liquid carbon dioxide are generated.
The patent system with the patent number 202110233126.3 solves the problem of carbon dioxide emission of hydrogen production by natural gas, uses carbon dioxide generated by reaction as a raw material to solve the problem of carbon dioxide source, changes waste into valuable, and realizes synchronous improvement of the material utilization rate and the energy utilization rate of the process system. However, the products of the process are hydrogen and liquid carbon dioxide, no electric energy is generated, and the process is applicable to a hydrogen production part of natural gas, and is different from the LNG cold energy utilization process provided by the patent.
The patent number 201721094836.8 discloses a process system for preparing dry ice by utilizing lng cold energy in liquefied natural gas power generation, which can effectively utilize combustion products, carbon dioxide and lng cold energy, realize cascade utilization of cold energy and carbon emission reduction, and has important significance of economy, energy conservation and emission reduction. However, the technology does not purify the liquefied carbon dioxide, and the generated electric energy is generated by natural gas combustion and is not a product of cold energy utilization.
Patent number 201510490793.4 discloses a system device and method for capturing liquefied carbon dioxide by utilizing liquefied natural gas cold energy. However, the process flow is complex, and is only suitable for the application of natural gas power plants, and the liquefied carbon dioxide is not subjected to purification treatment.
Patent number 201410425132.9 discloses a process for preparing liquid carbon dioxide and dry ice using LNG cold energy and an apparatus thereof. The process can realize gradient utilization of LNG cold energy, and the LNG cold energy utilization rate is high; the preparation pressure of the liquid CO 2 and the dry ice is reduced to 0.6-1.0 MPa by utilizing the cold energy of LNG, and the inlet gas CO 2 of the compressor is cooled to-40 to-30 ℃, so that the effect of saving energy by more than 58% compared with the common low-pressure method can be finally realized. However, the industrial product is single, no electric energy is generated, no liquid carbon dioxide purifying process is adopted in the process, and the produced liquid carbon dioxide cannot be used for industrial application.
Patent number 201310618307.3 discloses a combined power cycle method and system for capturing carbon dioxide using liquefied natural gas cold energy. However, the process flow is complex, and is suitable for the application of natural gas power plants, and the oxygen-enriched combustion also needs to prepare high-purity oxygen, so that the cost is increased.
Patent number 202310379259.0 discloses an LNG power ship energy comprehensive utilization system based on oxygen-enriched combustion carbon trapping, which comprises an air separation oxygen generation subsystem, a cold energy and waste heat utilization subsystem and a low-temperature carbon trapping subsystem. However, this patent is only suitable for LNG power vessels, the process is complicated, and the need for oxygen-enriched combustion to produce high purity oxygen results in increased costs.
The patent number 202220604871.4 proposes a device for deep recovery of carbon capture energy, which at least comprises an organic Rankine cycle power generation system, a CO 2 recovery system and an LNG cold energy regenerative system. The embodiment of the utility model can fully recover the low-grade heat of the low-pressure steam and the regenerated gas, and acquire a large amount of low-grade heat through an organic working medium and convert the low-grade heat into electric energy. However, the alcohol amine solution used in the process causes environmental pollution, a great amount of heat is supplied to a reboiler of the regeneration tower, and the process is complex and has more equipment.
Compared with the patent, the mixed working medium Rankine cycle is combined with the feed gas pre-expansion process, and the cold energy of the pressurized CO 2 is recovered, so that triple functions of liquefying and pressurizing the CO 2 and increasing the generated energy are realized, the cold energy can be more fully utilized, and the utilization efficiency of LNG cold energy is obviously improved. In addition, the ratio of power generation and liquefaction can be changed through a pre-expansion or compression process, and the high-purity liquid CO 2 is produced, so that the energy efficiency is high; the efficiency of the system is improved through specific matching of the proposed integrated process design with working media, components and process parameters; the refrigeration cycle is arranged between the condenser and the reboiler of the rectifying tower, LNG cold energy is utilized, the energy consumption of the refrigeration compressor is greatly reduced, and high-purity liquid carbon dioxide can be produced through coupling with the Rankine cycle.
Disclosure of Invention
In order to solve the defects in the prior art, the invention provides a method and a system for producing high-purity liquid CO 2 by utilizing LNG cold energy. The system provided by the invention comprises a CO 2 pressure treatment subsystem, a Rankine cycle subsystem and a rectification purification subsystem, wherein the CO 2 pressure treatment subsystem exchanges heat with working medium of the Rankine cycle subsystem through CO 2 gas outlet so as to provide energy required by working medium power generation and work application, and the rectification purification subsystem purifies the exchanged CO 2 gas outlet. The invention converts the pressure energy of partial raw material gas into electric energy by a split expansion mode aiming at the high-pressure CO 2 raw material gas which is conveyed by the pipe, thereby increasing the energy conversion efficiency of the process; aiming at the CO 2 feed gas with lower pressure which is conveyed by the pipe, the pressure of part of the feed gas is increased by a split-flow compression mode, so that the purpose of increasing the liquefaction amount of CO 2 is achieved. According to the rectification and purification subsystem, a refrigeration cycle is constructed between the condenser and the reboiler, LNG cold energy is recycled, and refrigeration energy consumption is greatly reduced.
According to the invention, CO 2 gas conveyed from a pipeline network is treated by expansion or pressurization modes according to different pressure values. In the system for liquefying CO 2 by utilizing LNG cold energy, the output of liquid CO 2 in the liquefaction separation system is improved through the coupling of methods such as split-flow expansion or split-flow compression of the inlet CO 2, directional matching with Rankine cycle working media and technological parameters, and the like, and the ratio between the liquefaction amount of CO 2 and the generated energy is adjusted according to the market demand. The method can change the ratio of power generation and liquefaction through a pre-expansion or compression process, and produce high-purity liquid CO 2, and has high energy efficiency; and the efficiency of the system is improved by specific matching of the proposed integrated process design with working media, components and process parameters.
The technical scheme provided by the invention is as follows:
a high purity liquid CO 2 production system utilizing LNG cold energy, comprising at least:
a first heat exchanger having a first flow passage, a second flow passage, a third flow passage, and a fourth flow passage;
A second heat exchanger having a first flow passage, a second flow passage, and a third flow passage;
a third heat exchanger having a first flow passage and a second flow passage;
the first tee joint, the first expander, the second tee joint and the first gas-liquid separator are sequentially communicated with each other and are provided with a carbon dioxide-containing pipeline, the first tee joint, the first expander, the second runner of the first heat exchanger, the first runner of the third heat exchanger, the second tee joint and the first gas-liquid separator; or comprises a first tee joint, a first compressor, a first cooler, a second tee joint and a first gas-liquid separator, wherein a carbon dioxide-containing pipeline, the first tee joint, the first compressor, the first cooler, a second runner of the first heat exchanger, a first runner of the third heat exchanger, the second tee joint and the first gas-liquid separator are sequentially communicated;
The working medium expander, the third flow passage of the second heat exchanger, the working medium pump, the first flow passage of the second heat exchanger, the second flow passage of the third heat exchanger and the third flow passage of the first heat exchanger are sequentially communicated, and the third flow passage of the first heat exchanger is also communicated with the working medium expander;
The liquefied natural gas inlet pipe, the third tee joint, the second runner of the second heat exchanger and the fourth runner of the first heat exchanger are sequentially communicated;
and the throttle valve, the carbon dioxide-containing pipeline, the first tee joint, the first runner of the first heat exchanger, the throttle valve and the second tee joint are sequentially communicated.
The high-purity liquid CO 2 production system utilizing LNG cold energy provided by the technical scheme can be used for generating power and liquefying carbon dioxide by taking a hydrocarbon mixture as a working medium, recycling liquefied natural gas cold energy and the like. The system takes low-temperature LNG as a low-temperature heat source, takes carbon dioxide and the like as high-temperature heat sources, and generates mechanical energy by recovering cold energy of the LNG and drives a generator to generate electricity.
The first expander, the heater and the second expander form a CO 2 expansion subsystem, the temperature of high-pressure carbon dioxide gas is reduced after expansion, then heat exchange is carried out under a certain pressure, impurities can be removed after the high-pressure carbon dioxide gas passes through a first liquid phase separator, the ratio of power generation and liquid CO 2 production can be changed, and the efficiency of the system is improved;
The first compressor, the first cooler, the second compressor and the second cooler form a CO 2 pressurizing subsystem, the temperature of low-pressure carbon dioxide gas is increased after the low-pressure carbon dioxide gas is compressed, then the low-pressure carbon dioxide gas exchanges heat under a certain pressure, impurities can be removed after the low-pressure carbon dioxide gas passes through a first liquid phase separator, the ratio of power generation and liquid CO 2 production can be changed, and the efficiency of the system is improved;
The CO 2 expansion subsystem and the CO 2 pressurization subsystem form a CO 2 pressure treatment system for treating the pressure of CO 2 gas conveyed by a pipeline;
The third flow passage of the first heat exchanger, the working medium expander, the third flow passage of the second heat exchanger, the working medium pump, the first flow passage of the second heat exchanger and the second flow passage of the third heat exchanger form a Rankine cycle system, and the circulating working medium is pressurized and expanded in the Rankine cycle system to generate electricity and exchange heat with the CO 2 gas;
LNG is delivered in a gaseous form after heat exchange by a heat exchanger.
Further, the high purity liquid CO 2 production system using LNG cold energy further includes:
the device comprises a rectifying tower, a condenser and a second gas-liquid separator, wherein the condenser is provided with a first flow passage and a second flow passage, a gas phase outlet of the rectifying tower, the first flow passage of the condenser and the second gas-liquid separator are sequentially communicated, and a liquid phase outlet of the second gas-liquid separator is also communicated with the upper part of the rectifying tower;
The reboiler is provided with a first flow passage, a second flow passage and a third flow passage, a liquid phase outlet of the rectifying tower, the first flow passage of the reboiler and the third gas-liquid separator are sequentially communicated, and a gas phase outlet of the third gas-liquid separator is also communicated with the lower part of the rectifying tower; the cooling water pipe is communicated with a second runner of the reboiler;
The refrigeration heat exchanger is provided with a first flow passage and a second flow passage, the refrigeration expander, the second flow passage of the refrigeration heat exchanger, the second flow passage of the condenser, the refrigeration compressor and the third flow passage of the reboiler are sequentially communicated, and the third flow passage of the reboiler is also communicated with the refrigeration expander; the liquefied natural gas inlet pipe, the third tee joint and the first flow passage of the refrigeration heat exchanger are sequentially communicated.
Based on the technical scheme, the purity of the carbon dioxide can be further improved through separation and rectification.
Further, the system further comprises a second expander, and the carbon dioxide-containing pipeline, the first tee joint, the first expander, the second expander and the second flow passage of the first heat exchanger are sequentially communicated.
Based on the technical scheme, the two-stage expansion is arranged, so that the liquefaction amount can be increased while the generated energy is further improved.
Further, the device also comprises a second compressor and a second cooler, wherein the carbon dioxide-containing pipeline, the first tee joint, the first compressor, the first cooler, the second compressor, the second cooler and the second flow passage of the first heat exchanger are sequentially communicated.
Based on the technical scheme, the liquefaction amount can be further increased by setting two-stage compression.
Specifically, the number of the tower plates of the rectifying tower is 16, and the inlet is arranged at the eighth tower plate; the liquid phase outlet of the second gas-liquid separator is connected with the first column plate of the rectifying column; the gas phase outlet of the third gas-liquid separator is connected with the sixteenth column plate of the rectifying column.
Based on the technical scheme, the energy consumption can be reduced, and the production efficiency is improved.
Specific:
The working medium of the working medium expander comprises ethane, propane and ethylene with the mol percent of (65-75)% (15-25)% (8-12)%. Preferably, the working medium of the working medium expander comprises 70 percent by mole of ethane, 20 percent by mole of propane and 10 percent by mole of ethylene;
the outlet conditions of the working medium at the working medium pump are as follows: -63.62 ℃,1.3mpa,130t/h, at the outlet conditions of the working medium expander are: -46.99 ℃,0.3MPa;
One air flow of the carbon dioxide-containing raw material gas is subjected to heat exchange by the first heat exchanger and then is reduced to the temperature of-21.37 ℃, the other air flow of the carbon dioxide-containing raw material gas is subjected to heat exchange by the first heat exchanger and the second heat exchanger and then is reduced to the temperature of-23.66 ℃, and the temperature of the two air flows is-21.98 ℃ after being combined;
the temperature of one air flow of the liquefied natural gas is increased to-75.21 ℃ after passing through the second heat exchanger and the first heat exchanger, and the temperature of one air flow of the liquefied natural gas is increased to-4.86 ℃ after passing through the refrigeration heat exchanger;
the outlet pressure of the rectifying tower is 1.9 to 2MPa, preferably 1.95MPa, and the top pressure is 1.8 to 1.9MPa, preferably 1.9MPa.
The above process conditions constitute boundary conditions for the operation of the system, and are mutually matched and cross-affected. The high cold energy utilization efficiency can be ensured by reasonably adjusting the proportion of the mixed working medium and matching with the technological parameters such as the expansion pressure of the raw material gas.
The ratio between the liquefied product and the power generation is flexibly regulated, the carbon dioxide is split and expanded through the raw material and the rectifying tower is split and compressed, and the ratio of the carbon dioxide liquefaction and the power generation can be regulated by changing the split ratio.
The heat exchange of cold and hot fluid in the heat exchanger can form a plurality of echelons through the split expansion of the raw material gas and the split compression of the top of the rectifying tower, and the heat exchange of the cold and hot fluid in the heat exchanger is integrated with the specific composition of the Rankine cycle working medium and the specific range of the technological parameters, so that the heat exchange in the heat exchanger can be improved, the irreversible loss is reduced, and the efficiency of the whole system is improved.
The invention also provides a method for producing the high-purity liquid CO 2 by utilizing the LNG cold energy, and the system for producing the high-purity liquid CO 2 by utilizing the LNG cold energy provided by the invention is used for carrying out the following steps: the liquefied natural gas is used as a cold source to prepare the high-purity liquid CO 2, and the working medium expander is used for generating power, and the liquefaction and rectification part is used for producing the high-purity liquid CO 2 with efficiency exceeding the existing level under the matching of refrigeration, separation, working medium, components, flow and parameters, so that the energy consumption is low, the running cost is low and the benefit is good.
The invention has the beneficial effects that:
The invention has the advantages that CO 2 liquefaction, CO 2 pressurization and power generation can be simultaneously realized in the same flow, and the flow is simple and the efficiency is high;
The CO 2 is subjected to depressurization and expansion in advance before cooling and heat exchange, and then the mixed working medium is used for carrying out Rankine cycle heat exchange and cooling; whether in the field of natural gas liquefaction or the field of LNG cold energy utilization, the conventional thinking is to pressurize CO 2 first and then liquefy the CO 2. According to the invention, the raw material gas is depressurized and expanded before entering the low-temperature heat exchanger for cooling, so that the generated energy can be effectively increased, the LNG cold energy can be more fully utilized, and the efficiency of utilizing the LNG cold energy is further improved;
The invention can realize the full and efficient utilization of cold energy, and is obtained by organically combining a plurality of measures such as mixed working medium Rankine cycle, CO 2 expansion cooling or pressurizing heating process, specific composition and proportion of mixed working medium, specific value ranges of a plurality of technological parameters and the like, wherein each measure is organically combined into a whole, and is inseparable;
the invention can also carry out rectification on the separated smoke components to obtain purer CO 2 gas;
The invention combines the advantages of compression or expansion, shallow low-temperature liquefaction and rectification, can separate impurities with the boiling point similar to that of CO 2, ensures that low-concentration CO 2 raw material gas containing various impurities obtains higher-concentration CO 2, and further removes other impurities to obtain high-purity industrial-grade liquid CO 2 or food additive liquid CO 2; the integrated system can reasonably realize liquefaction and separation of high-pressure or low-pressure carbon dioxide, has good adaptability and reliability, has the characteristics of pressure energy recovery and multistage heat exchange, and can generate electricity;
the design energy consumption of the rectifying part is low, and the production efficiency can be improved.
Drawings
Fig. 1 is a system diagram of a high purity liquid CO 2 production system utilizing LNG cold energy for high pressure carbon dioxide provided by the present invention.
Fig. 2 is a system diagram of a high purity liquid CO 2 production system utilizing LNG cold energy for low pressure carbon dioxide provided by the present invention.
In fig. 1 and 2, the contents represented by the respective reference numerals are as follows:
the incoming gas of the pipeline is respectively as follows: 1.2, 3, 5, 6, 7, 8, 9, 10, 11, 35, 36, 29;
The liquid CO 2 is respectively: 12. 13, 14, 15, 16, 17, 30, 31, 32, 33, 34;
LNG is: 18. 19, 20, 21, 22;
Cooling water: 37.
Detailed Description
The principles and features of the present invention are described below with examples only to illustrate the present invention and not to limit the scope of the present invention.
In the following examples, the isentropic efficiency of the compressor was 0.75, the turbine efficiency was 0.85, and the pump efficiency was 0.75.
The LNG vaporization unit includes a first two heat exchangers and a first heat exchanger along the LNG flow direction.
The carbon dioxide liquefying unit passes through the first expander, the second expander, the first heat exchanger and the third heat exchanger, enters the rectifying tower for purification, and LNG is subjected to heat exchange through the second heat exchanger and the first heat exchanger in sequence and then is output.
The comprehensive utilization system provided in this embodiment further includes a heater disposed on the outlet of the first expander.
9.3MPa of LNG at the temperature of minus 138 ℃ and 200t/h of LNG delivered by the LNG receiving station is delivered to a second heat exchanger, heat exchange is carried out between the LNG and the mixed cycle working medium in the second heat exchanger, and the temperature of the LNG after heat exchange is increased to minus 64.17 ℃;
The LNG after temperature rising enters a first heat exchanger, exchanges heat with the mixed cycle working medium and the carbon dioxide gas in the first heat exchanger, and the temperature of the LNG after heat exchange is raised to-34.43 ℃ and is fed into a long-distance pipeline network for transmission;
The mixed working medium enters a second heat exchanger to exchange heat with LNG entering the second heat exchanger, and the mixed working medium exchanges heat and is cooled to-49.12 ℃;
The liquefying amount of the carbon dioxide can reach 367.9t/h, and the liquefying amount is reduced along with the increase of the temperature of the inlet flue gas.
Example 1
The embodiment provides a production process of high-purity liquid CO 2 by utilizing LNG cold energy, and the structure of the production process is shown in figure 1:
The system comprises: the CO 2 expansion power generation system, the Rankine cycle system and the rectification purification system; the CO 2 expansion power generation system is used for converting partial pressure energy of raw material gas into electric energy, and the depressurized carbon dioxide gas enters a first heat exchanger of the Rankine cycle and exchanges heat with a circulating working medium to be liquefied; the system specifically comprises a first expander, a heater and a second expander which are connected in sequence; the circulating working medium is pressurized and expanded in a Rankine cycle system to generate power; the circulation is completed by sequentially passing through a third flow passage of the first heat exchanger, a working medium expander, a third flow passage of the second heat exchanger, a working medium pump, the first flow passage of the second heat exchanger and the second flow passage of the third heat exchanger; after passing through the tee joint, one LNG passes through the second runner of the second heat exchanger and the fourth runner of the first heat exchanger in sequence to complete gasification, and the other LNG passes through the refrigeration heat exchanger to complete gasification; the expanded CO 2 flow passes through the second flow passage of the first heat exchanger and the first flow passage of the third heat exchanger and then is mixed with the unexpanded CO 2 flow after passing through the first heat exchanger and the throttle valve, the mixture is introduced into the gas-liquid separator, and the liquid CO 2 flows out of the bottom of the gas-liquid separator and enters the rectifying tower for purification; the rectification and purification system is responsible for removing impurities in the liquid CO 2 and ensuring the purity of the liquid CO 2; the refrigeration cycle of the rectification purification system provides energy for the rectification tower; the device specifically comprises a refrigeration heat exchanger, a rectifying tower condenser, a refrigeration compressor, a rectifying tower reboiler and a refrigeration expander which are connected in sequence.
The CO 2 feed gas composition was methane 2.23%, ethane 0.12%, carbon dioxide 96.98%, nitrogen 0.67% (mole percent); in a CO 2 gas expansion pipeline, the temperature is reduced to-19.98 ℃ from 7000kPa to 2010kPa through two stages of expansion pressure, then the gas enters a first heat exchanger for cooling and liquefying, the temperature is reduced to-21.23 ℃, then the gas enters a third heat exchanger for further cooling, and the temperature is reduced to-21.37 ℃; in a CO 2 gas unexpanded pipeline, cooling by a first heat exchanger, reducing the temperature to 0 ℃, reducing the pressure by a throttle valve, reducing the pressure from 6995kPa to 2000kPa, and reducing the temperature to-23.66 ℃; the two pipelines are mixed and enter a gas-liquid separator, liquid CO 2 flows out of the bottom of the separator and enters a rectifying tower for purification, high-purity liquid CO 2 flows out of the bottom of a reboiler of the rectifying tower after purification, the components are CO 2 99.98.98% and ethane 0.02% (mol percent), the pressure is 1950kPa, and the liquid carbon dioxide product is sent into a storage tank for storage.
The Rankine cycle system comprises the following steps:
the Rankine cycle working medium is a mixture and consists of 70% of ethane, 20% of propane and 10% (mole percent) of ethylene.
The Rankine cycle working medium is pressurized to 1167kPa by a working medium pump, then sequentially passes through a second heat exchanger, a third heat exchanger and a first heat exchanger, the temperatures are respectively increased to-49 ℃ to-51 ℃, 48 ℃ to-50 ℃ and 6 ℃ to-8 ℃, the working medium becomes pure gas phase and then enters an expander to perform work and power generation, the pressure is reduced to 300kPa, the working medium enters the second heat exchanger to absorb LNG and cold energy liquefaction of the cycle working medium after the temperature is reduced, and enters the pump to be pressurized after the working medium becomes liquid state, so that the cycle is completed.
The refrigerating cycle of the rectification and purification system comprises the following steps:
The refrigeration cycle working medium of the rectification and purification system is propane.
The refrigerating cycle working medium of the rectification purification system is pressurized to 720kPa by a refrigerating compressor, then the high-pressure flow enters a rectifying tower reboiler for heat exchange, the temperature is reduced to 38 ℃ to 42 ℃ after heat exchange, then the high-pressure flow enters a refrigerating expansion machine for power generation, the pressure is reduced to 150kPa, the low-pressure flow enters a refrigerating heat exchanger for absorbing LNG cold energy for liquefaction, finally the low-pressure flow enters a rectifying tower condenser for heat exchange, the temperature is increased to minus 28 ℃ to 30 ℃, and then the high-pressure flow enters the refrigerating compressor for circulation.
Physical properties of each flow node in this example are shown in table 1.
TABLE 1
The performance achieved by this example is shown in table 2.
TABLE 2
Example 2
The present embodiment provides a process for producing high-purity liquid CO 2 using LNG cold energy, which is different from example 1 in that the pressure of carbon dioxide supplied from the pipe is low, and the structure is as shown in fig. 2:
The system comprises: CO 2 pressurizing system, rankine cycle system and rectifying and purifying system; the CO 2 pressurizing system is used for increasing the pressure of part of raw material gas, so that the liquefying amount of carbon dioxide can be increased; the pressurized carbon dioxide gas enters a first heat exchanger of the Rankine cycle and exchanges heat with a circulating working medium to be liquefied; the device specifically comprises a first compressor, a heater and a second compressor which are sequentially connected; the circulating working medium is pressurized and expanded in a Rankine cycle system to generate power; the circulation is completed by sequentially passing through a third flow passage of the first heat exchanger, a working medium expander, a third flow passage of the second heat exchanger, a working medium pump, the first flow passage of the second heat exchanger and the second flow passage of the third heat exchanger; after passing through the tee joint, one LNG passes through the second runner of the second heat exchanger and the fourth runner of the first heat exchanger in sequence to complete gasification, and the other LNG passes through the refrigeration heat exchanger to complete gasification; the pressurized CO 2 flow passes through the second flow passage of the first heat exchanger and the first flow passage of the third heat exchanger and then is mixed with the uncompressed CO 2 flow after passing through the first heat exchanger and the throttle valve, the mixture is introduced into the gas-liquid separator, and the liquid CO 2 flows out from the bottom of the gas-liquid separator and enters the rectifying tower for purification; the rectification and purification system is responsible for removing impurities in the liquid CO 2 and ensuring the purity of the liquid CO 2; the refrigeration cycle of the rectification purification system provides energy for the rectification tower; the device specifically comprises a refrigeration heat exchanger, a rectifying tower condenser, a refrigeration compressor, a rectifying tower reboiler and a refrigeration expander which are connected in sequence.
The CO 2 feed gas composition was methane 2.23%, ethane 0.12%, carbon dioxide 96.98%, nitrogen 0.67% (mole percent); in a CO 2 gas pressurizing pipeline, the temperature is increased to 62.07 ℃ from 2000kPa to 4000kPa through two stages of compression pressure, then the gas is cooled and liquefied in a first heat exchanger, the temperature is reduced to-6.2 ℃, then the gas is further cooled in a third heat exchanger, the temperature is reduced to-11.31 ℃, the gas is reduced in pressure through a throttle valve, the pressure is reduced from 3985kPa to 1995kPa, and the temperature is reduced to-25.57 ℃; in a CO 2 gas non-pressurizing pipeline, cooling by a first heat exchanger, and then cooling to-42.78 ℃; the two pipelines are mixed and enter a gas-liquid separator, liquid CO 2 flows out of the bottom of the separator and enters a rectifying tower for purification, high-purity liquid CO 2 flows out of the bottom of a reboiler of the rectifying tower after purification, the components are CO 2 99.98.98% and ethane 0.02% (mol percent), the pressure is 1950kPa, and the liquid carbon dioxide product is sent into a storage tank for storage.
The Rankine cycle system comprises the following steps:
the Rankine cycle working medium is a mixture and consists of 70% of ethane, 20% of propane and 10% (mole percent) of ethylene.
The Rankine cycle working medium is pressurized to 905kPa by a working medium pump, then sequentially passes through a second heat exchanger, a third heat exchanger and a first heat exchanger, the temperatures are respectively increased to-60 ℃,55 ℃ and-15.95 ℃, the working medium becomes pure gas phase and then enters an expander to perform work and power generation, the pressure is reduced to 239kPa, the working medium enters the second heat exchanger to absorb LNG and the cold energy of the cycle working medium to liquefy after the temperature is reduced, and the working medium enters the pump to be pressurized after the working medium becomes liquid, so that the cycle is completed.
The refrigerating cycle of the rectification and purification system comprises the following steps:
The refrigeration cycle working medium of the rectification and purification system is propane.
The refrigerating cycle working medium of the rectification purification system is pressurized to 1000kPa by a refrigerating compressor, then the high-pressure flow enters a rectifying tower reboiler for heat exchange, the temperature is reduced to 40 ℃ after heat exchange, then the high-pressure flow enters a refrigerating expander for power generation by working, the pressure is reduced to 150kPa, the low-pressure flow enters a refrigerating heat exchanger for absorbing LNG cold energy for liquefaction, finally the low-pressure flow enters a rectifying tower condenser for heat exchange, the temperature is increased to-27.70 ℃, and then the high-pressure flow enters the refrigerating compressor for circulation.
Physical properties of each flow node in this example are shown in table 3.
TABLE 3 Table 3
The performance achieved by this example is shown in table 4.
TABLE 4 Table 4
| Process for producing a solid-state image sensor | Compression | Expansion of |
| Liquid CO 2 yield (kg/h) | 295600 | 261500 |
| CO 2 concentration in the product (%) | 99.98 | 99.98 |
| Recovery of CO 2 (%) | 73.9 | 65.37 |
| Technological energy consumption (kW) | 2339.95 | 1045.6 |
| Art generating capacity (kW) | 2532.2 | 4971.16 |
| Rankine cycle generating capacity (kW) | 1894 | 3547 |
| Net generating capacity (kW) | 192.25 | 3925.56 |
| CO 2 liquefaction Rate (kg/kg LNG) | 1.478 | 1.307 |
The foregoing description of the preferred embodiments of the invention is not intended to limit the invention to the precise form disclosed, and any such modifications, equivalents, and alternatives falling within the spirit and scope of the invention are intended to be included within the scope of the invention.
Claims (8)
1. A high purity liquid CO 2 production system utilizing LNG cold energy, comprising at least:
a first heat exchanger having a first flow passage, a second flow passage, a third flow passage, and a fourth flow passage;
A second heat exchanger having a first flow passage, a second flow passage, and a third flow passage;
a third heat exchanger having a first flow passage and a second flow passage;
the first tee joint, the first expander, the second tee joint and the first gas-liquid separator are sequentially communicated with each other and are provided with a carbon dioxide-containing pipeline, the first tee joint, the first expander, the second runner of the first heat exchanger, the first runner of the third heat exchanger, the second tee joint and the first gas-liquid separator; or comprises a first tee joint, a first compressor, a first cooler, a second tee joint and a first gas-liquid separator, wherein a carbon dioxide-containing pipeline, the first tee joint, the first compressor, the first cooler, a second runner of the first heat exchanger, a first runner of the third heat exchanger, the second tee joint and the first gas-liquid separator are sequentially communicated;
The working medium expander, the third flow passage of the second heat exchanger, the working medium pump, the first flow passage of the second heat exchanger, the second flow passage of the third heat exchanger and the third flow passage of the first heat exchanger are sequentially communicated, and the third flow passage of the first heat exchanger is also communicated with the working medium expander;
The liquefied natural gas inlet pipe, the third tee joint, the second runner of the second heat exchanger and the fourth runner of the first heat exchanger are sequentially communicated;
and the throttle valve, the carbon dioxide-containing pipeline, the first tee joint, the first runner of the first heat exchanger, the throttle valve and the second tee joint are sequentially communicated.
2. The high purity liquid CO 2 production system utilizing LNG cold energy of claim 1, wherein: the system also comprises a rectifying tower, a condenser, a second gas-liquid separator, a refrigeration expansion machine, a refrigeration heat exchanger and a refrigeration compressor, wherein the condenser is provided with a first flow passage and a second flow passage, a gas phase outlet of the rectifying tower, the first flow passage of the condenser and the second gas-liquid separator are sequentially communicated, and a liquid phase outlet of the second gas-liquid separator is also communicated with the upper part of the rectifying tower; the refrigeration heat exchanger is provided with a first flow passage and a second flow passage, the refrigeration expansion machine, the second flow passage of the refrigeration heat exchanger, the second flow passage of the condenser and the refrigeration compressor are sequentially communicated, and the refrigeration compression is also communicated with the refrigeration expansion machine; the liquefied natural gas inlet pipe, the third tee joint and the first flow passage of the refrigeration heat exchanger are sequentially communicated.
3. The high purity liquid CO 2 production system using LNG cold energy of claim 2, wherein: the system also comprises a reboiler, a third gas-liquid separator and a cooling water pipe, wherein the reboiler is provided with a first flow passage, a second flow passage and a third flow passage, a liquid phase outlet of the rectifying tower, the first flow passage of the reboiler and the third gas-liquid separator are sequentially communicated, and a gas phase outlet of the third gas-liquid separator is also communicated with the lower part of the rectifying tower; the cooling water pipe is communicated with a second runner of the reboiler; the refrigeration compressor, the third runner of the reboiler and the refrigeration expander are sequentially communicated; the number of the tower plates of the rectifying tower is 16, and the inlet is arranged at the eighth tower plate; the liquid phase outlet of the second gas-liquid separator is connected with the first column plate of the rectifying column; the gas phase outlet of the third gas-liquid separator is connected with the sixteenth column plate of the rectifying column.
4. The high purity liquid CO 2 production system using LNG cold energy according to claim 3, wherein: the system also comprises a second expander, wherein the carbon dioxide-containing pipeline, the first tee joint, the first expander, the second expander and the second flow passage of the first heat exchanger are sequentially communicated.
5. The high purity liquid CO 2 production system using LNG cold energy according to claim 3, wherein: the system further comprises a second compressor and a second cooler, wherein the carbon dioxide-containing pipeline, the first tee joint, the first compressor, the first cooler, the second compressor, the second cooler and the second flow passage of the first heat exchanger are sequentially communicated.
6. The high purity liquid CO 2 production system using LNG cold energy according to any one of claims 1 to 5, wherein:
The working medium of the working medium expander comprises ethane, propane and ethylene with the mol percent of (65-75)% (15-25)% (8-12)%; or the working medium of the working medium expander comprises ethane, propane and ethylene with the mole percentage of 70 percent to 20 percent to 10 percent;
the outlet conditions of the working medium at the working medium pump are as follows: -63.62 ℃,1.3mpa,130t/h, at the outlet conditions of the working medium expander are: -46.99 ℃,0.3MPa;
One air flow of the carbon dioxide-containing raw material gas is subjected to heat exchange by the first heat exchanger and then is reduced to the temperature of-21.37 ℃, the other air flow of the carbon dioxide-containing raw material gas is subjected to heat exchange by the first heat exchanger and the second heat exchanger and then is reduced to the temperature of-23.66 ℃, and the temperature of the two air flows is-21.98 ℃ after being combined;
the temperature of one air flow of the liquefied natural gas is increased to-75.21 ℃ after passing through the second heat exchanger and the first heat exchanger, and the temperature of one air flow of the liquefied natural gas is increased to-4.86 ℃ after passing through the refrigeration heat exchanger;
the outlet pressure of the rectifying tower is 1.9-2 MPa of the bottom pressure and 1.8-1.9 MPa of the top pressure.
7. A method for producing high-purity liquid CO 2 using LNG cold energy, characterized by using the high-purity liquid CO 2 production system using LNG cold energy according to any one of claims 1 to 6, comprising the steps of: liquefied natural gas is used as a cold source to prepare high-purity liquid CO 2, and the high-purity liquid CO 2 is subjected to work-producing power generation through a working medium expander.
8. The method for producing high purity liquid CO 2 using LNG cold energy according to claim 7, wherein:
In a CO 2 gas expansion pipeline, the temperature is reduced to-18 ℃ to-20 ℃ from 7000kPa to 2010kPa through two stages of expansion pressure, then the gas enters a first heat exchanger for cooling and liquefying, the temperature is reduced to-20 ℃ to-21 ℃, then the gas enters a third heat exchanger for further cooling, and the temperature is reduced to-21 ℃ to-23 ℃; in a CO 2 gas unexpanded pipeline, cooling by a first heat exchanger, reducing the temperature to-1 ℃ to 1 ℃, reducing the pressure by a throttle valve, reducing the pressure from 6995kPa to 2000kPa, and reducing the temperature to-22 ℃ to-24 ℃; mixing the two pipelines, then, entering a gas-liquid separator, allowing liquid CO 2 to flow out of the bottom of the gas-liquid separator, entering a rectifying tower for purification, allowing high-purity liquid CO 2 to flow out of the bottom of a rectifying tower reboiler after purification, and allowing the liquid CO 2 to be composed of CO 2 99.98.98% and ethane 0.02% in mole percentage, wherein the pressure is 1950kPa, and allowing a liquid carbon dioxide product to be sent into a storage tank for storage;
In a CO 2 gas pressurizing pipeline, the pressure is increased from 2000kPa to 4000kPa through two stages of compression, the temperature is increased to 60 ℃ to 64 ℃, the temperature is initially reduced through a condenser, then the temperature is reduced to minus 5 ℃ to minus 8 ℃ through a first heat exchanger, then the temperature is further reduced through a third heat exchanger, the temperature is reduced to minus 10 ℃ to minus 12 ℃, the pressure is reduced through a throttle valve, the pressure is reduced from 3985kPa to 1995kPa, and the temperature is reduced to minus 23 ℃ to minus 27 ℃; in a CO 2 gas non-pressurizing pipeline, cooling by a first heat exchanger, and then cooling to-40 ℃ to-43 ℃; the two pipelines are mixed and enter a gas-liquid separator, liquid CO 2 flows out of the bottom of the gas-liquid separator and enters a rectifying tower for purification, high-purity liquid CO 2 flows out of the bottom of a rectifying tower reboiler after purification, the components of the high-purity liquid CO 2 are CO 2 99.98.98% and ethane 0.02% according to mole percentage, the pressure is 1950kPa, and the liquid carbon dioxide product is sent into a storage tank for storage.
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