CN105115245B - The system and device and its method of liquefied carbon dioxide are trapped using cold energy of liquefied natural gas - Google Patents
The system and device and its method of liquefied carbon dioxide are trapped using cold energy of liquefied natural gas Download PDFInfo
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- CN105115245B CN105115245B CN201510490793.4A CN201510490793A CN105115245B CN 105115245 B CN105115245 B CN 105115245B CN 201510490793 A CN201510490793 A CN 201510490793A CN 105115245 B CN105115245 B CN 105115245B
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- flue gas
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- carbon dioxide
- propane
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 188
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 112
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 88
- 239000003949 liquefied natural gas Substances 0.000 title claims abstract description 87
- 238000000034 method Methods 0.000 title claims abstract description 34
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims abstract description 108
- 239000001294 propane Substances 0.000 claims abstract description 56
- 239000002918 waste heat Substances 0.000 claims abstract description 48
- 239000000779 smoke Substances 0.000 claims abstract description 35
- 230000005611 electricity Effects 0.000 claims abstract description 25
- 238000011084 recovery Methods 0.000 claims abstract description 23
- 239000002737 fuel gas Substances 0.000 claims abstract description 14
- 239000003517 fume Substances 0.000 claims abstract description 12
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 123
- 239000003546 flue gas Substances 0.000 claims description 123
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 72
- 239000003345 natural gas Substances 0.000 claims description 38
- 238000002485 combustion reaction Methods 0.000 claims description 34
- 239000007789 gas Substances 0.000 claims description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 26
- 239000007788 liquid Substances 0.000 claims description 15
- 238000001816 cooling Methods 0.000 claims description 14
- 239000000567 combustion gas Substances 0.000 claims description 11
- 239000002808 molecular sieve Substances 0.000 claims description 10
- 230000009467 reduction Effects 0.000 claims description 9
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 9
- 235000019504 cigarettes Nutrition 0.000 claims description 7
- 239000008246 gaseous mixture Substances 0.000 claims description 5
- 238000002309 gasification Methods 0.000 claims description 5
- 238000001179 sorption measurement Methods 0.000 claims description 4
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 3
- 239000003570 air Substances 0.000 claims description 2
- 238000010438 heat treatment Methods 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 16
- 238000005057 refrigeration Methods 0.000 abstract description 3
- 230000007613 environmental effect Effects 0.000 abstract 1
- 229960004424 carbon dioxide Drugs 0.000 description 76
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 12
- 229910052799 carbon Inorganic materials 0.000 description 12
- 230000008569 process Effects 0.000 description 12
- 235000011089 carbon dioxide Nutrition 0.000 description 10
- 238000000926 separation method Methods 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 239000002803 fossil fuel Substances 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 230000008859 change Effects 0.000 description 5
- 238000003860 storage Methods 0.000 description 5
- 230000005540 biological transmission Effects 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 3
- 239000002671 adjuvant Substances 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 241000790917 Dioxys <bee> Species 0.000 description 2
- GCNLQHANGFOQKY-UHFFFAOYSA-N [C+4].[O-2].[O-2].[Ti+4] Chemical compound [C+4].[O-2].[O-2].[Ti+4] GCNLQHANGFOQKY-UHFFFAOYSA-N 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 238000002955 isolation Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000003507 refrigerant Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229940063664 carbon dioxide 10 % Drugs 0.000 description 1
- UBAZGMLMVVQSCD-UHFFFAOYSA-N carbon dioxide;molecular oxygen Chemical compound O=O.O=C=O UBAZGMLMVVQSCD-UHFFFAOYSA-N 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- -1 flue gas F-GAS11) Chemical compound 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000003292 glue Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- SOQBVABWOPYFQZ-UHFFFAOYSA-N oxygen(2-);titanium(4+) Chemical class [O-2].[O-2].[Ti+4] SOQBVABWOPYFQZ-UHFFFAOYSA-N 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titanium dioxide Inorganic materials O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
- 235000010215 titanium dioxide Nutrition 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 230000007306 turnover Effects 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- 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
-
- 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
- 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
- F25J1/0221—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 using the cold stored in an external cryogenic component in an open refrigeration loop
- F25J1/0222—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 using the cold stored in an external cryogenic component in an open refrigeration loop in combination with an intermediate heat exchange fluid between the cryogenic component and the fluid to be liquefied
-
- 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
- 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
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
- F25J1/023—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the combustion as fuels, i.e. integration with the fuel gas system
-
- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
-
- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/70—Flue or combustion exhaust gas
-
- 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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/30—Compression of the feed stream
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
The invention discloses a kind of system and device of utilization cold energy of liquefied natural gas trapping liquefied carbon dioxide and its method.The system and device includes LNG cold energy and reclaimed and pressure energy recovery system, and fuel gas buring is generated electricity, fume waste heat is reclaimed and generated electricity and three parts of smoke circulating system and smoke carbon dioxide separating-purifying and propane cycles carbon dioxide liquefaction system.By the way that LNG cold energy is reclaimed and pressure energy recovery system, fuel gas generation technology and CO2Liquefaction trapping triplicity, has not only reclaimed LNG cold energy, meanwhile, conventional refrigeration device is eliminated, CO is reduced2Liquefaction trapping cost, realizing LNG cold energy, efficiently variation is utilized, and efficiency of energy utilization is improved, with obvious environmental benefit, economic benefit, social benefit.
Description
Technical field
Utilized the invention belongs to cold energy of liquefied natural gas and carbon dioxide discharge-reduction field, and in particular to one kind utilizes the day that liquefies
Right air cooling can trap the system and device and its method of liquefied carbon dioxide.
Background technology
LNG and its cold energy use：Liquefaction is a kind of feasible pattern for transporting natural gas, is transported using adiabatic LNG storage tank
Liquefied natural gas has turned into the important means of modern natural gas trade.The liquefied natural gas that transport comes is in the pressurized rear gas of receiving station
Change and enter gas ductwork transmission ＆ distribution, the cold that this process has about 800KJ/kg discharges.Eighties of last century the nineties, people are
Begin one's study the technology of LNG gasification cold energy recycle, and current LNG cold energy is primarily used to air separation, lighter hydrocarbons separation, cold energy
In terms of generating, collecting carbonic anhydride and dry ice preparation, freezer, desalinization and low-temperature grinding.
In the last few years, China LNG entered the fast-developing phase, and coastal receiving station's construction has started climax one by one.At present
Building up the receiving station put into operation has 6,24,200,000 tons/year of receiving ability.Check and approve and building 6,21,500,000 tons of receiving ability of design/
Year, separately there are 6 receiving stations to achieve the Committee of Development and Reform " travel permit " file, carry out previous work, it is contemplated that overall design receiving ability
17200000 tons/year.In this correspondence, a collection of LNG and its cold energy use industry are have accumulated around LNG receiving stations.With Putian, fujian Province
Exemplified by LNG receiving stations, surrounding has built up Putian plant gas, cold energy use space division factory and fine glue powder factory in succession.However, with day
Sheet, South Korea etc. compare, and China's LNG cold energy uses starting is relatively later, single using form, there was only cold energy space division and rubber at present
Deep cooling crush realizes industrialization, and other cold energy use technologies are still in conceptual phase.
CO2 emission and emission reduction：Carbon dioxide is the common recognition that a kind of greenhouse gases have arrived people, with industry
The process of change, the mankind create the summation more than the wealth of society before modern age with the time of nearly 200 years, and associated in this is big
Great amount of carbon dioxide will be discharged after measuring the burning of the fossil fuels such as coal, oil, natural gas, these combustion of fossil fuel.According near
Generation research shows that global temperature rise alreadys exceed 0.6 DEG C over nearly 100 years, if continued for, it is contemplated that to the middle of this century, the whole world
Temperature will raise 1.5~4.5 DEG C, and coastal cities will not exist all over the world at that time.This problem gradually causes people's
Concern, and the action of reply climate change is made that, it has been recognized that global temperature will effectively be slowed down by reducing CO2 emission
Rise.European Union, Japan and other countries take the lead in starting carbon emissions trading, to reduce the discharge of carbon dioxide.
In terms of climate change is tackled, China is also made that huge effort.First, Copenhagen climate change in 2009
Shortly before conference, the Chinese government is made that responsible promise to the world：To the year two thousand twenty China unit GDP titanium dioxide
Carbon emission declined 40%~45% than 2005.Secondly, carbon emissions trading is actively developed, emission reduction mesh is realized with the means in market
's.Reopened after a cessation of business in succession as the transaction pilot of carbon emission in advance Beijing, Guangdong, Shanghai, Tianjin, Chongqing, Hubei and the provinces and cities of Shenzhen 7,
At the year end of cut-off 2014, seven big pilot secondary market turnovers break through 5.3 hundred million yuan.At the beginning of 2014, national relevant ministries and commissions leader is just
National carbon emissions trading market is released by the signal of operation in 2016 in different occasions.December 12, the Committee of Development and Reform was sent out then
Cloth《Carbon emissions trading manages Tentative Measures》, the whole process to national carbon emissions trading done detailed regulation, extremely
This Chinese carbon market initially enters countdown.
In future, carbon emission power will turn into a kind of hard trading product.Multiple rows of is cost, and emission reduction is income, how to pass through carbon
Emission reduction additional income has become the problem that enterprise needs to study.
Collecting carbonic anhydride and liquefaction：Collecting carbonic anhydride divides after being divided into pre-combustion separation and burning according to technology path
From.Pre-combustion separation technology is the characteristic that hydrocarbon two kinds of elements are rich in using fossil fuel, is separated the two by chemically reacting,
The fuel based on hydrogen is made, while separating carbon dioxide.The technology is primarily present in the preparation process of commercial syngas at present,
Fossil fuel generates the synthesis gas based on hydrogen and carbon dioxide by steam reforming transformationreation, and separating-purifying obtains pure
Net hydrogen and carbon dioxide.
After burning isolation technics according to the difference of carbon dioxide in flue gas concentration after burning can be divided into again conventional combustion and
Oxygen-enriched combusting.Conventional combustion is the combustion technology that fossil fuel is carried out using air as combustion adjuvant, the flue gas that this method is obtained
Middle carbon dioxide content is relatively low, and generally below 15%, it need to subsequently be equipped with pressure-swing absorption apparatus, amine aqueous solution absorption plant or UF membrane
Device etc. separates purifying carbon dioxide.Oxygen-enriched combustion technology is that fossil fuel fires under the combustion adjuvant that pure oxygen and circulating flue gas are constituted
Burn, the combustion technology of the content of carbon dioxide in flue gas is improved by flue gas recirculation, this method carbon dioxide in flue gas is utilized
Concentration can reach more than 95%.
Whether pre-combustion separation technology or burning after isolation technics, obtained carbon dioxide is present with gaseous state,
This brings great inconvenience to storage, transport, and for the ease of storage, transport, the carbon dioxide trapped above needs further
Liquefaction.
Pressurized carbon dioxide is reduced to 2.5~3.0MPa by traditional liquefaction process, is recycled refrigeration plant cooling and is liquefied.And
Using LNG cold energy, then the low temperature required for cooling and liquefied carbon dioxide is readily available, so that by the work of liquefying plant
Pressure is down to 0.9MPa or so.Compared with traditional liquefaction process, the load of refrigeration plant is greatly reduced, and power consumption is also reduced
30%~40%.
Chinese patent 201020000778.X gives a kind of conventional coal-burning power plant's collecting carbonic anhydride technology, and it utilizes second
Alkanolamine solution absorbing carbon dioxide, obtains separating-purifying, but the technique lacks co 2 liquefaction process, lacks remote fortune
Defeated possibility.
United States Patent (USP) US7637109B2 gives a kind of oxygen-enriched combustion technology, passes through the control burning that adds water in a combustion chamber
Temperature, produces high temperature and high pressure flue gas and promotes turbine acting, and the flue gas after acting is cooled down using LNG and separates carbon dioxide, the program
The trapping of carbon dioxide is realized, but does not consider the comprehensive utilization of energy, whole efficiency is relatively low.
201310618307.3 pairs of such schemes of Chinese invention patent (application number) are improved, and are utilizing oxygen-enriched combusting skill
On the basis of art, the waste heat that waste heat boiler reclaims flue gas after acting is with the addition of, while using LNG condensing trapping carbon dioxide, it is real
Show on the basis of collecting carbonic anhydride, improved the total energy efficiency of device.But the program needs to increase air separation unit
Pure oxygen is prepared, equipment overall investment is big, and unit liquid carbon dioxide cost is higher.
Chinese invention patent (application number) 02107780.0 gives LNG cold energy under a kind of conventional combustion and traps carbon dioxide
Technology.It is sublimated the carbon dioxide in flue gas using the cold energy of LNG gasification, and the carbon dioxide for condensing in heat exchanger outer wall passes through
Two row parallel tube heat exchangers blocked operations are recycled, but it is larger that unit carbon dioxide LNG cold energy consumptions are trapped in the program.
Chinese invention patent (application number) 201110073906.2 gives a kind of low by the generation of flue gas choke heat drop
The scheme of temperature trapping carbon dioxide, the program eliminates purifying carbon dioxide process, but choke pressure is higher, and air compression takes
With and finishing operations it is costly, and collecting carbonic anhydride rate is relatively low, about 10%.
The content of the invention
It is an object of the invention to provide a kind of utilization cold energy of liquefied natural gas trapping liquefied carbon dioxide system and device and
Its method.
System and device provided by the present invention, including LNG cold energy are reclaimed and pressure energy recovery system, fuel gas buring generating,
Fume waste heat, which is reclaimed, to generate electricity and smoke circulating system and smoke carbon dioxide separating-purifying and propane cycles co 2 liquefaction system
Three parts of system,
Wherein, the LNG cold energy reclaim and pressure energy recovery system in waste heat boiler be denoted as B16 and the fuel gas buring
Generate electricity, the waste heat boiler that fume waste heat is reclaimed in generating and smoke circulating system is denoted as B15 and is connected；
Heat exchanger in the LNG cold energy recovery and pressure energy recovery system is denoted as B29 and fuel gas buring generating, cigarette
Combustion reactor in the generating of gas Waste Heat Recovery and smoke circulating system is denoted as B13 and is connected；
The smoke carbon dioxide separating-purifying is distinguished with propane cycles carbon dioxide liquefaction system by waste heat boiler B16
Generated electricity with LNG cold energy recovery and pressure energy recovery system and the fuel gas buring, fume waste heat reclaims generating and flue gas is followed
Waste heat boiler B15 in loop system is connected.
In said system device, the LNG cold energy is reclaimed and pressure energy recovery system is denoted as B24, changed including LNG high-pressure pumps
Hot device is denoted as B25, condenser and is denoted as B26, current divider and is denoted as B27, waste heat boiler B16, combustion gas turbine being denoted as B28 and heat exchanger
B29；The LNG high-pressure pumps B24, heat exchanger B25, condenser B26, current divider B27, waste heat boiler B16, combustion gas turbine B28 and
Heat exchanger B29 is sequentially connected.
The fuel gas buring is generated electricity, fume waste heat reclaims generating and smoke circulating system is denoted as including flue gas air mixer
B11, air compressor are denoted as B12, combustion reactor B13, smoke gas turbine and are denoted as B14 and steam rankine cycle electricity generation system；Institute
Flue gas air mixer B11, air compressor B12, combustion reactor B13, smoke gas turbine B14 and steam rankine cycle is stated to generate electricity
System is sequentially connected,
Wherein, the steam rankine cycle electricity generation system is denoted as B20, middle pressure including waste heat boiler B15, high-pressure steam turbine
Steam turbine is denoted as that B21, condenser are denoted as B22 and water circulating pump is denoted as B23；The waste heat boiler B15, high-pressure steam turbine
B20, middle pressure steam turbine B21, condenser B22 and water circulating pump B23 are sequentially connected.
The smoke carbon dioxide separating-purifying is separated with smoke carbon dioxide in propane cycles carbon dioxide liquefaction system
Purification system includes waste heat boiler B16, cooler and is denoted as B17, gas-liquid separator and is denoted as B18, current divider being denoted as B19, compressor
It is denoted as B30, heat exchanger and is denoted as B31, molecular sieve dehydrater being denoted as B32 and CO2Purifying system is denoted as B33；The waste heat pot
Stove B16, cooler B17, gas-liquid separator B18, current divider B19, compressor B30, heat exchanger B31, molecular sieve dehydrater B32 and
CO2Purifying system B33 is sequentially connected,
Wherein, the smoke carbon dioxide separating-purifying and propane cycles dioxy in propane cycles carbon dioxide liquefaction system
Changing carbon liquefaction system includes CO2Liquefier is denoted as that B36, propane cycles pump are denoted as B37 and heat exchanger is denoted as B25；The CO2Liquefaction
Device B36, propane cycles pump B37 and heat exchanger B25 are sequentially connected.
Method provided by the present invention, comprises the following steps：
1) air is denoted as F-GAS16 with circulating flue gas and is mixed to get gaseous mixture, and gaseous mixture is denoted as NG7 with natural gas and mixed again
Close, burn, generation flue gas is denoted as F-GAS1, flue gas F-GAS1 does work into turbine, and the flue gas after acting is denoted as F-GAS2；
Flue gas F-GAS2 enters the boiler of steam rankine cycle system, and steam raising obtains steam note to recirculated water in the boiler
Make STEAM-1, steam STEAM-1 is done work by turbine, and the steam after acting is denoted as STEAM-2；Steam STEAM-2 enters again
Enter the boiler heating of steam rankine cycle system, obtain steam and be denoted as STEAM-3, steam STEAM-3 is done work by turbine, done
Steam after work(is denoted as STEAM-4；Steam STEAM-4 is all condensed into aqueous water and circulated again through circulating pump pressurization；From steam
The flue gas discharged in rankine cycle system is denoted as F-GAS3；
Flue gas F-GAS3 is denoted as NG4 with natural gas and exchanged heat, and the natural gas after heat exchange is denoted as NG5, the flue gas after heat exchange
It is denoted as F-GAS4；
2) liquefied natural gas is pressurized exchanges heat with propane, the propane temperature reduction after heat exchange, LNG temperature rise,
Gasify as high-pressure natural gas, be denoted as NG1；
High-pressure natural gas NG1 enters distributing system through final temperature adjustment, and the high-pressure natural gas into distributing system is denoted as NG2；
Natural gas NG2 is divided into two strands, and one is denoted as NG3, and another stock is denoted as NG4；NG3 is directly entered urban pipe network；
NG4 is exchanged heat with flue gas F-GAS3, and the flue gas after heat exchange is denoted as F-GAS4, and the natural gas after heat exchange is denoted as NG5,
Natural gas NG5 is done work by turbine；Natural gas after acting mixes with circulating flue gas and air through temperature adjustment, burnt.
3) the condensed devices of flue gas F-GAS4 are cooled to normal temperature, and the flue gas after cooling is denoted as F-GAS5；
Flue gas F-GAS5 removes condensed water through gas-liquid separator, and obtained flue gas is denoted as F-GAS6；Flue gas F-GAS6 is divided into
Two strands, one is used as circulating flue gas and air and natural gas mixed combustion, and another stock is used to reclaim carbon dioxide；For reclaiming
The flue gas of carbon dioxide is denoted as F-GAS7；
Flue gas F-GAS7 once boosts through compressor to be obtained flue gas and is denoted as F-GAS8, through cooling down water cooling, molecular sieve depth
Water removal obtains pure flue gas F-GAS10；
Flue gas F-GAS10 enters Pressure Swing Adsorption system (including absorption and desorption) and obtains rich carbonated cigarette
Gas, is denoted as F-GAS11, and flue gas F-GAS11 obtains flue gas F-GAS13 through the cooling of compressor secondary booster；
Flue gas F-GAS13 and liquefied natural gas precooling, temperature reduction obtain the flue gas F-GAS14 and step 1 of cold) third
Co 2 liquefaction in propane heat exchange in alkane circulation, flue gas, is denoted as L-CO2；
In the above method, step 1) in, the air is 10 with circulating flue gas F-GAS16 volume ratio:(5~7).
The temperature of the flue gas F-GAS1 is 1200~1350 DEG C.
The temperature of the flue gas F-GAS2 is 550~700 DEG C, and pressure is 1.1~1.5atm.
The temperature of the flue gas F-GAS13 is 20~35 DEG C, and pressure is 8~9atm.The flue gas F-GAS6 is divided into two strands,
The volume ratio of circulating flue gas and the flue gas F-GAS7 is 1:(1~2).
In the above method, step 2) in, the propane pressurizes through propane cycles pump, and pressure rise is denoted as C3H8-1；Pressurization
Propane afterwards, which enters heat exchanger and LNG heat-exchange temperatures, to be reduced, and is denoted as C3H8- 2, propane and the step 3 of temperature reduction) in F-GAS14
Final heat-exchange temperature rise, is denoted as C3H8-3；Propane C3H8- 3, which are again introduced into the pressurization of propane cycles pump, completes whole circulation.It is described
The temperature of propane C3H8-2 after heat exchange is -70~-50 DEG C.
The cold energy discharged when the present invention is using liquefied natural gas gasifying has incorporated plant gas come liquefied carbon dioxide
Generated electricity with cold energy of liquefied natural gas.The program improves carbon dioxide in flue gas concentration by part of smoke circulation, reduces
The investment cost of carbon dioxide in flue gas purifier, provides low temperature using LNG cold energy, reduces co 2 liquefaction device
Investment and operating cost, while improving the generating efficiency of LNG cold energy using the UTILIZATION OF VESIDUAL HEAT IN of flue gas.The program can be used for newly-built
The cold energy use planning of LNG receiving stations, can be used for the plant gas transformation for relying on LNG receiving stations to build.
Compared with prior art, the present invention has the advantages that：
1) present invention cooks combustion adjuvant using air, without pure oxygen, eliminates air separation unit.
2) the variation utilization of LNG cold energy is realized：In the last few years, cold energy of liquefied natural gas gradually obtained people using technology
Attention, China sea oil has built up domestic first set LNG cold energy air separation units in Putian, fujian Province, but LNG cold energy titanium dioxides
Carbon trapping technique is still in theory and technology conceptual phase, and unrealized industrialization, herein by LNG cold energy uses and CO2Liquefaction trapping
With reference to not only realizing the recovery of LNG cold energy, and liquid carbon dioxide production cost is reduced, realize LNG cold energy efficiently many
Sampleization is utilized.
3) cold transmission safety：Herein in cold transfer stages by LNG- propane heat exchangers, realize LNG colds to
CO2The safety transmission of liquefaction unit, while the introducing of middle refrigerant propane adds CO2The operating flexibility of liquefaction unit, it is to avoid
Carbon dioxide is because of the risk of low temperature frozen plug pipeline.
4) equipment operation expense is low：The carbon dioxide in flue gas concentration of conventional gas turbines is relatively low, and this programme uses part
The scheme of flue gas recirculation adds the concentration of carbon dioxide in flue gas, and this reduces follow-up flue gas treating process to a certain extent
Cost of equipment and finishing operations expense.
5) system effectiveness is high：This programme is by gas turbine power generation, and LNG cold energy uses, co 2 liquefaction, NG pressure energies are sharp
The efficient utilization of energy efficiency is realized with integrating, system whole efficiency is up to 45.7%.
Brief description of the drawings
Fig. 1 is the process chart of cold energy of liquefied natural gas trapping liquefaction plant gas carbon dioxide in embodiment 1, its
In, B11- air flue gas blenders；B12- air compressors；B13- combustion reactors；B14- smoke gas turbines；B15- waste heat boilers
Stove；B16- waste heat boilers；B17- coolers；B18- gas-liquid separators；B19- current dividers；B20- high-pressure steam turbines；In B21-
Press steam turbine；B22- coolers；B23- water circulating pumps；B24-LNG pumps；B25- heat exchangers；B26- condensers；B27- is shunted
Device；B28- combustion gas turbines；B29- heat exchangers；B30- compressors；B31- heat exchangers；B32- molecular sieve dehydraters；B33-CO2Purification
Cleaning system；B34- compressors；B35- condensers；B36-CO2Liquefier；B37- propane cycles pumps.
Embodiment
The method of the present invention is illustrated below by specific embodiment, but the invention is not limited in this.
Experimental method described in following embodiments, unless otherwise specified, is conventional method；The reagent and material, such as
Without specified otherwise, commercially obtain.
In following embodiments, compressor, combustion gas turbine, flue gas turbine expander turbine, the isentropic efficiency of steam turbine take 0.9, machine
Tool efficiency takes 0.95, and the efficiency of pump takes 0.95, and mechanical efficiency takes 0.9, and scheme puts aside device pressure drop.
In following embodiments, the cold fire of 1atm, -161 DEG C of LNG is with for 402.3KJ/Kg.
In following embodiments, methane Lower heat value 35.99MJ/Nm3。
In following embodiments, formula used is as follows：
Generating efficiency=net power output/(gas consumption X natural gases status calorific value)
Overall efficiency=net power output/(gas consumption X natural gases status calorific value+LNG measures the cold fire of XLNG units
With)
Embodiment 1, method and its system using liquefied natural gas (LNG) cold energy trapping carbon dioxide：
First, the system that carbon dioxide is trapped using cold energy of liquefied natural gas, its system architecture is as shown in Figure 1：It is cold including LNG
It can reclaim and pressure energy recovery system, fuel gas buring generates electricity, fume waste heat reclaims generate electricity (steam circulation electricity generation system) and flue gas
The circulatory system and smoke carbon dioxide separating-purifying and three parts of propane cycles carbon dioxide liquefaction system.
Wherein, the LNG cold energy is reclaimed and pressure energy recovery system includes LNG high-pressure pumps B24, heat exchanger B25, condenser
It is denoted as B26, current divider B27, waste heat boiler B16, combustion gas turbine B28 and heat exchanger B29；The LNG high-pressure pumps B24, heat exchanger
B25, condenser B26, current divider B27, waste heat boiler B16 (i.e. smoke gas afterheat heat exchanger), combustion gas turbine B28 (i.e. NG turbines) and
Heat exchanger B29 is sequentially connected.
The fuel gas buring, which generates electricity, fume waste heat reclaims generating (steam circulation electricity generation system) and smoke circulating system includes
Flue gas air mixer B11, air compressor B12, combustion reactor B13, smoke gas turbine B14 and steam rankine cycle, which generate electricity, is
System；The flue gas air mixer B11, air compressor B12, combustion reactor B13, smoke gas turbine B14 and steam Lang Ken are followed
Ring electricity generation system is sequentially connected.
Wherein, the steam rankine cycle electricity generation system includes waste heat boiler B15, high-pressure steam turbine B20, middle pressure steam
Turbine B21, condenser B22 and water circulating pump B23；The waste heat boiler B15, high-pressure steam turbine B20, middle pressure steam turbine
B21, condenser B22 and water circulating pump B23 are sequentially connected.
The smoke carbon dioxide separating-purifying is separated with smoke carbon dioxide in propane cycles carbon dioxide liquefaction system
Purification system includes waste heat boiler B16, cooler B17, gas-liquid separator B18, current divider B19, compressor B30, heat exchanger
B31, molecular sieve dehydrater B32 and CO2Purifying system B33；The waste heat boiler B16, cooler B17, gas-liquid separator
B18, current divider B19, compressor B30, heat exchanger B31, molecular sieve dehydrater B32 and CO2Purifying system B33 connects successively
Connect.
Wherein, the smoke carbon dioxide separating-purifying and propane cycles dioxy in propane cycles carbon dioxide liquefaction system
Changing carbon liquefaction system includes CO2Liquefier B36, propane cycles pump B37 and heat exchanger B25；The CO2Liquefier B36, propane are followed
Ring pump B37 and heat exchanger B25 are sequentially connected.
2nd, the method that carbon dioxide is trapped using liquefied natural gas (LNG) cold energy, process chart is as shown in Figure 1：
1) plant gas generates electricity：500,000Nm under the status of criterion3/ h air (AIR) with from step 2) 330,
000Nm3/ h circulating flue gas F-GAS16 is well mixed in air flue gas blender B11, is boosted to through air compressor B12
13~20atm, specifically boosts to 17atm.
Come from LNG gasification section 25000Kg/h, 30 DEG C, 17bar natural gas NG7 and gaseous mixture are denoted as F-GAS18 and entered
Enter 1280 DEG C of burning generation in combustion reactor B13,17bar high temperature and high pressure flue gas F-GAS1, high temperature and high pressure flue gas promotes cigarette
Gas turbine B14 does work, and temperature is down to 630 DEG C, and pressure is down to 1.3atm.
Above-mentioned steps are conventional plant gas electrification technique, and smoke gas turbine B14 coaxially does work with air compressor B12, always
Generated output is 119.3MW.
The flue gas F-GAS2 discharged from smoke gas turbine B14 enters steam rankine cycle system, reclaims its remaining heat.
Comprise the following steps that：
Flue gas F-GAS2 temperature is 630 DEG C after acting, the 240t/h from water circulating pump B23 (i.e. boiler feed pump),
18MPa, 105 DEG C of recirculated water in waste heat boiler (B15) with flue gas heat exchange, through heat exchange, evaporation, overheat, recirculated water is in used heat
580 DEG C are produced in boiler B15,18MPa superheated steam STEAM-1, flue gas F-GAS2 temperature is down to 110 DEG C or so.High steam
STEAM-1, which enters in high-pressure steam turbine B20, to do work, and the pressure flowed out from steam turbine is 7MPa, and temperature drops for its temperature
To 350 DEG C.Then heat is absorbed in waste heat boiler B15 again steam STEAM-2 is sent back to, temperature rises to 530 DEG C.By steam
STEAM-3 delivers to middle pressure steam turbine B21 actings, and temperature drop is to 120 DEG C, and pressure drops to 1.2atm.Through cooler B22
(i.e. cooling tower) is cooled down, and steam STEAM-4 is all condensed into aqueous water, and aqueous water is pressurized through water circulating pump B23, is delivered to useless again
Utilization is circulated in heat boiler B15.
The step completes a complete steam rankine cycle, and net generated output is 65.7MW.
2) LNG cold energy is reclaimed and pressure energy generates electricity：
LNG is stored in LNG storage tank with normal pressure (1atm) state, and temperature is -161 DEG C.To reach transmission ＆ distribution requirement, it is necessary to will
LNG is forced into ductwork pressure.
LNG's from storage tank 30t/h is forced into 8MPa through pump B24, into heat exchanger B25 and step 3) in 500t/h
Propane (C3H8-1) exchanges heat.LNG gasification is high-pressure gas in this step, and propane temperature is down to -65 DEG C.In order to further improve
Capacity usage ratio, high-pressure gas and step 3) in the high-pressure carbon dioxide of purification exchange heat, temperature rises to zero degree, titanium dioxide
Carbon is cooled to -30 DEG C.After the step, combustion gas is matched somebody with somebody through last temperature adjustment into distributing system remote conveying.
Into distributing system 8MPa natural gases NG2 current divider B27 punishment separate out two strands, one natural gas NG3 is direct
Into urban pipe network, another gang of 7Kg/s natural gas NG4 is used for gas turbine combustion.The operating pressure of gas turbine is
17atm, this gang of natural gas NG4, which need to enter after pressure regulation in the B13 of combustion reaction room, to burn.In order to improve generating efficiency and follow-up
Gas turbine combustion efficiency, this gang of natural gas NG4 again with step 1) in close to normal pressure flue gas F-GAS3 in waste heat boiler B16
Middle progress secondary heat exchange raises temperature to 95 DEG C, and combustion gas NG5 is passed into combustion gas turbine B28 expansion works, and pressure is down to 17atm
Afterwards, combustion power generation in combustion reactor (gas-turbine combustion chamber) is entered.
The step can reclaim for gaseous-pressure, and net generated output is 1.5MW.
3) LNG cold energy carries out co 2 liquefaction trapping：
The flue gas F-GAS3 discharged from waste heat boiler B15 enters in waste heat boiler B16, is discharged from waste heat boiler B16
Flue gas F-GAS4 temperature is connected to nearly 105 DEG C, and the most of vapor being cooled to through cooler B17 in normal temperature, flue gas liquefies, by cigarette
Gas F-GAS5 removes condensed water therein by gas-liquid separator B18, obtains flue gas F-GAS6, and flue gas composition is nitrogen
83%, oxygen 5%, carbon dioxide 10%.
Flue gas F-GAS6 is passed through into current divider B19 by volume 1:1 point be two strands, one be used for step 1) in air mix
Close, for circulating combustion, another stock is used for collecting carbonic anhydride.
330,000Nm is separated through current divider B193/ h flue gas F-GAS7 is used to reclaim carbon dioxide, and flue gas F-GAS7 leads to
4atm is forced into overcompression machine B30, cooler B31 cooled flue gas is set to normal temperature, flue gas F-GAS9 warps in compressor outlet
The water removal of molecular sieve dehydrater B32 depth obtains the pure flue gas based on nitrogen, oxygen, carbon dioxide, then passes it through CO2Carry
Sublimate system B33 (Pressure Swing Adsorption workshop section includes the techniques such as adsorption and desorption) processing, obtains purity more than 95%
Carbon dioxide (i.e. flue gas F-GAS11), the rate of recovery 85% of the step carbon dioxide.
Flue gas F-GAS11 is pressurized to 9atm through compressor B34, sets condenser to be denoted as B35 cooling cigarettes in compressor end
Gas, flue gas F-GAS13 enters precooling in condenser B26, and temperature is down to -30 DEG C, and last flue gas F-GAS14 enters CO2Liquefier
Liquefied in B36, remove nitrogen and oxygen of residual etc., obtain liquefied carbon dioxide (L-CO2), -50 DEG C of temperature, purity 98%,
The rate of recovery 95% of this step carbon dioxide.
Liquid carbon dioxide as needed can be through the follow-up deep processing process of refinement of row.
In upper step, co 2 liquefaction processing workshop section includes the cyclic process one using propane as refrigerant.The third of 500t/h
Alkane is forced into 3atm through propane cycles pump B37, is exchanged heat into LNG- propane heat exchanger B25 and LNG, and temperature is down to -65 DEG C, obtained
The propane of cold enters CO2F-GAS14 heat exchange is denoted as with being cooled to -30 DEG C of carbon dioxide in advance in liquefier B36, carbon dioxide is inhaled
It is liquid carbon dioxide (L-CO to receive cold liquefaction2), temperature is -50 DEG C, and propane pressurizes through propane cycles pump B37, is again introduced into
Whole circulation is completed in LNG- propane heat exchangers.
According to above-mentioned technique, after the power consumption 24WM for deducting compressor and pump, system net power output is 162.5WM.According to
Generating efficiency and comprehensive energy efficiency formula, calculate the method for comprehensive utilization cold energy of liquefied natural gas trapping liquefied carbon dioxide and its are
The generating efficiency of system is 46.2%, and comprehensive energy efficiency is 45.7%, recovery rate of CO 2 81%.
Claims (7)
1. a kind of utilization cold energy of liquefied natural gas traps the system and device of liquefied carbon dioxide, including LNG cold energy is reclaimed and pressure
Can recovery system, fuel gas buring generating, fume waste heat recovery generating and smoke circulating system and smoke carbon dioxide separating-purifying
With three parts of propane cycles carbon dioxide liquefaction system；
Wherein, the LNG cold energy reclaim and the waste heat boiler (B16) in pressure energy recovery system and fuel gas buring generating,
The waste heat boiler (B15) that fume waste heat is reclaimed in generating and smoke circulating system is connected；
The LNG cold energy is reclaimed and the heat exchanger (B29) in pressure energy recovery system and fuel gas buring generating, fume waste heat
The combustion reactor (B13) reclaimed in generating and smoke circulating system is connected；
The smoke carbon dioxide separating-purifying and propane cycles carbon dioxide liquefaction system by waste heat boiler (B16) respectively with
The LNG cold energy is reclaimed and pressure energy recovery system and fuel gas buring generating, fume waste heat recovery generating and flue gas recirculation
Waste heat boiler (B15) in system is connected.
2. system and device according to claim 1, it is characterised in that：The LNG cold energy is reclaimed and pressure energy recovery system
Including LNG high-pressure pumps (B24), heat exchanger (B25), condenser (B26), current divider (B27), waste heat boiler (B16), combustion gas turbine
And heat exchanger (B29) (B28)；It is the LNG high-pressure pumps (B24), heat exchanger (B25), condenser (B26), current divider (B27), remaining
Heat boiler (B16), combustion gas turbine (B28) and heat exchanger (B29) are sequentially connected.
3. system and device according to claim 1 or 2, it is characterised in that：The fuel gas buring is generated electricity, fume waste heat is reclaimed
Generate electricity and smoke circulating system includes flue gas air mixer (B11), air compressor (B12), combustion reactor (B13), cigarette
Gas turbine (B14) and steam rankine cycle electricity generation system；The flue gas air mixer (B11), air compressor (B12), combustion
Reactor (B13), smoke gas turbine (B14) and steam rankine cycle electricity generation system is burnt to be sequentially connected；
Wherein, the steam rankine cycle electricity generation system includes waste heat boiler (B15), high-pressure steam turbine (B20), middle pressure steam
Turbine (B21), condenser (B22) and water circulating pump (B23)；The waste heat boiler (B15), high-pressure steam turbine (B20), middle pressure
Steam turbine (B21), condenser (B22) and water circulating pump (B23) are sequentially connected.
4. system and device according to claim 1 or 2, it is characterised in that：The smoke carbon dioxide separating-purifying and third
Smoke carbon dioxide system for separating and purifying includes waste heat boiler (B16), cooler in alkane circulation carbon dioxide liquefaction system
(B17), gas-liquid separator (B18), current divider (B19), compressor (B30), heat exchanger (B31), molecular sieve dehydrater (B32) and
CO2Purifying system (B33)；The waste heat boiler (B16), cooler (B17), gas-liquid separator (B18), current divider
(B19), compressor (B30), heat exchanger (B31), molecular sieve dehydrater (B32) and CO2Purifying system (B33) connects successively
Connect；
The smoke carbon dioxide separating-purifying and propane cycles co 2 liquefaction in propane cycles carbon dioxide liquefaction system
System includes CO2Liquefier (B36), propane cycles pump (B37) and heat exchanger (B25)；The CO2Liquefier (B36), propane are followed
Ring pump (B37) and heat exchanger (B25) are sequentially connected.
5. trapping the method for carbon dioxide using the system and device any one of claim 1-4, comprise the following steps：
1) air is mixed to get gaseous mixture with circulating flue gas F-GAS16, and gaseous mixture mixes with natural gas NG7, burnt again, generates cigarette
Gas F-GAS1, flue gas F-GAS1 are done work into turbine, and flue gas F-GAS2 is obtained after acting；
Flue gas F-GAS2 enters the boiler of steam rankine cycle system, and steam raising obtains steam STEAM- to recirculated water in the boiler
1, steam STEAM-1 is done work by turbine, and steam STEAM-2 is obtained after acting；Steam STEAM-2 is again introduced into steam Lang Ken
The boiler heating of the circulatory system, obtains steam STEAM-3, and steam STEAM-3 is done work by turbine, and steam is obtained after acting
STEAM-4；Steam STEAM-4 is all condensed into aqueous water and circulated again through circulating pump pressurization；From steam rankine cycle system
Discharge flue gas F-GAS3；
Flue gas F-GAS3 is exchanged heat with natural gas NG4, and natural gas NG5 and flue gas F-GAS4 are obtained after heat exchange；
2) liquefied natural gas is pressurized exchanges heat with propane, the propane temperature reduction after heat exchange, LNG temperature rise, gasification
For high-pressure natural gas NG1；
High-pressure natural gas NG1 enters distributing system through final temperature adjustment, and the high-pressure natural gas into distributing system is natural gas NG2；
Natural gas NG2 is divided into two strands, and one is natural gas NG3, and another stock is natural gas NG4；Natural gas NG3 is directly entered city
Pipe network；
Natural gas NG4 is exchanged heat with flue gas F-GAS3, and flue gas F-GAS4 and natural gas NG5 are obtained after heat exchange, and natural gas NG5 leads to
Cross turbine acting；Natural gas after acting mixes with circulating flue gas and air through temperature adjustment, burnt；
3) the condensed devices of flue gas F-GAS4, which are cooled to after normal temperature, cooling, obtains flue gas F-GAS5；
Flue gas F-GAS5 removes condensed water, obtains flue gas F-GAS6 through gas-liquid separator；Flue gas F-GAS6 is divided into two strands, one
As circulating flue gas and air and natural gas mixed combustion, another stock is used to reclaim carbon dioxide；For reclaiming carbon dioxide
Flue gas is flue gas F-GAS7；
Flue gas F-GAS7 is once boosted through compressor and obtains flue gas F-GAS8, and through cooling down water cooling, the water removal of molecular sieve depth is obtained
Pure flue gas F-GAS10；
Flue gas F-GAS10 obtains rich carbonated flue gas F-GAS11, flue gas F-GAS11 into Pressure Swing Adsorption system
Flue gas F-GAS13 is obtained through the cooling of compressor secondary booster；
Flue gas F-GAS13 and liquefied natural gas precooling, temperature reduction, obtain the flue gas F-GAS14 and step 1 of cold) propane follows
Carbon dioxide liquid in propane heat exchange in ring, flue gas turns to carbon dioxide L-CO2.
6. method according to claim 5, it is characterised in that：Step 1) in, the air is with circulating flue gas F-GAS16's
Volume ratio is 10:(5~7)；
The temperature of the flue gas F-GAS1 is 1200~1350 DEG C；
The temperature of the flue gas F-GAS2 is 550~700 DEG C, and pressure is 1.1~1.5atm；
The temperature of the flue gas F-GAS13 is 20~35 DEG C, and pressure is 8~9atm；
The flue gas F-GAS6 is divided into two strands, and the volume ratio of circulating flue gas and the flue gas F-GAS7 is 1:(1~2).
7. the method according to claim 5 or 6, it is characterised in that：Step 2) in, the propane adds through propane cycles pump
Pressure, pressure rise obtains propane C3H8-1；Propane C after pressurization3H8- 1, which enters heat exchanger and LNG heat-exchange temperatures, reduces, and obtains
Propane C3H8- 2, the propane C of temperature reduction3H8- 2 with step 3) in the final heat-exchange temperatures of flue gas F-GAS14 raise, obtain propane
C3H8-3；Propane C3H8- 3, which are again introduced into the pressurization of propane cycles pump, completes whole circulation；Propane C after the heat exchange3H8- 2 temperature
Spend for -70~-50 DEG C.
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| CN103867894A (en) * | 2014-03-29 | 2014-06-18 | 辽宁石油化工大学 | Method and device for generating power and capturing CO2 through cold energy of liquefied natural gas |
| CN203743849U (en) * | 2014-03-29 | 2014-07-30 | 辽宁石油化工大学 | Device for generating and collecting carbon dioxide (CO2) by utilizing liquefied natural gas cold energy |
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Effective date of registration: 20221021 Address after: No. 293, Tanggu East 6th Road, Binhai New Area, Tianjin 300456 Patentee after: CNOOC Energy Development Co.,Ltd. Clean Energy Branch Address before: 102200 CNOOC Research Institute, future science and Technology City, Changping District, Beijing Patentee before: BEIJING COLD ENERGY UTILIZATION INSTITUTE OF CNOOC ENERGY TECHNOLOGY & SERVICE LTD. |