CN105115245A - System device for trapping liquefied carbon dioxide by using cold energy of liquefied natural gas and method of device - Google Patents
System device for trapping liquefied carbon dioxide by using cold energy of liquefied natural gas and method of device Download PDFInfo
- Publication number
- CN105115245A CN105115245A CN201510490793.4A CN201510490793A CN105115245A CN 105115245 A CN105115245 A CN 105115245A CN 201510490793 A CN201510490793 A CN 201510490793A CN 105115245 A CN105115245 A CN 105115245A
- Authority
- CN
- China
- Prior art keywords
- denoted
- flue gas
- steam
- carbon dioxide
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 201
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 97
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 92
- 239000003949 liquefied natural gas Substances 0.000 title claims abstract description 88
- 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 106
- 239000002918 waste heat Substances 0.000 claims abstract description 51
- 239000000779 smoke Substances 0.000 claims abstract description 41
- 238000002485 combustion reaction Methods 0.000 claims abstract description 34
- 238000011084 recovery Methods 0.000 claims abstract description 22
- 230000005611 electricity Effects 0.000 claims abstract description 19
- 239000002737 fuel gas Substances 0.000 claims abstract description 14
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 121
- 239000003546 flue gas Substances 0.000 claims description 121
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 69
- 239000001294 propane Substances 0.000 claims description 56
- 239000003345 natural gas Substances 0.000 claims description 33
- 239000007789 gas Substances 0.000 claims description 28
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 23
- 239000007788 liquid Substances 0.000 claims description 15
- 239000003517 fume Substances 0.000 claims description 13
- 239000000567 combustion gas Substances 0.000 claims description 11
- 239000002808 molecular sieve Substances 0.000 claims description 10
- 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
- 238000001816 cooling Methods 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 6
- 239000008246 gaseous mixture Substances 0.000 claims description 5
- 238000001179 sorption measurement Methods 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 2
- 238000010791 quenching Methods 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 16
- 238000000926 separation method Methods 0.000 abstract description 7
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 238000005057 refrigeration Methods 0.000 abstract description 3
- 238000000746 purification Methods 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 abstract 1
- 229960004424 carbon dioxide Drugs 0.000 description 82
- 230000008569 process Effects 0.000 description 14
- 235000011089 carbon dioxide Nutrition 0.000 description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 9
- 229910052799 carbon Inorganic materials 0.000 description 9
- 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
- 238000003860 storage Methods 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 4
- 238000002955 isolation 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
- 239000002671 adjuvant Substances 0.000 description 3
- 230000005540 biological transmission Effects 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 238000002309 gasification Methods 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
- 230000009467 reduction Effects 0.000 description 3
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 2
- 229910002090 carbon oxide Inorganic materials 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
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 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
- 238000012546 transfer Methods 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
- 230000009286 beneficial effect Effects 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
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003245 coal Substances 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
- 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
- 238000007726 management method Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000000630 rising effect Effects 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
- 230000009466 transformation Effects 0.000 description 1
- 238000001926 trapping method Methods 0.000 description 1
- 230000007306 turnover Effects 0.000 description 1
Classifications
-
- 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
Landscapes
- 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 system device for trapping liquefied carbon dioxide by using cold energy of liquefied natural gas and a method of the device. The system device comprises an LNG (Liquefied Natural Gas) cold energy recovery and pressure energy recovery system, a fuel gas combustion electricity production, smoke waste heat recovery electricity production and smoke circulation system and a smoke and carbon dioxide separation and purification, dimethylmethane circulation and carbon dioxide liquefying system. The LNG cold energy recovery and pressure energy recovery system, a fuel gas electricity production technology and a carbon dioxide liquefying and trapping are combined, so that the LNG cold energy is recovered, and at the same time, conventional refrigeration devices are avoided, the carbon dioxide liquefying and trapping cost is reduced, efficient and diversified utilization of the LNG cold energy is realized, the energy utilization rate is increased, and remarkable environmental benefits, economic benefits and social benefits are obtained.
Description
Technical field
The invention belongs to cold energy of liquefied natural gas to utilize and carbon dioxide discharge-reduction field, be specifically related to a kind of system and device and the method thereof that utilize cold energy of liquefied natural gas trapping liquefied carbon dioxide.
Background technology
LNG and cold energy use thereof: liquefaction is a kind of feasible pattern of transport natural gas, use adiabatic LNG storage tank conveying liquified natural gas to become the important means of modern natural gas trade.The liquefied natural gas that transport comes enters gas ductwork transmission & distribution in receiving station's gasification after pressurization, and this process has the cold of about 800KJ/kg to discharge.Eighties of last century the nineties, the people LNG that begun one's study gasifies the technology of cold energy recycle, and current LNG cold energy is mainly used to the aspects such as air separation, lighter hydrocarbons separation, cold energy generation, 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 the construction of coastal receiving station has started climax one by one.The built receiving station put into operation has 6, receiving ability 2,420 ten thousand tons/year at present.Check and approve and building 6, design receiving ability 2,150 ten thousand tons/year, separately has 6 receiving stations to achieve the Committee of Development and Reform's " travel permit " file, carries out previous work, estimates overall design receiving ability 1,720 ten thousand tons/year.Corresponding in this, have accumulated a collection of LNG and cold energy use industry thereof round LNG receiving station.For Putian, fujian Province LNG receiving station, Putian plant gas, the empty subsidiary factory of cold energy use and fine glue powder factory are in succession built up around.But compared with Japan, Korea S etc., China LNG cold energy use starting is relatively late, utilizes form single, only have cold energy sky point to achieve industrialization with rubber deep cooling crush at present, other cold energy use technology is still in conceptual phase.
CO2 emission and reduction of discharging: carbon dioxide is that a kind of greenhouse gases have arrived the common recognition of people, along with industrialized process, the mankind with time of nearly 200 years create exceed modern age before the summation of the wealth of society, what accompany in this is the burning of the fossil fuels such as a large amount of coal, oil, natural gas, will discharge great amount of carbon dioxide after these combustion of fossil fuel.Show according to recent studies, over nearly 100 years, global temperature rise is more than 0.6 DEG C, if continue to continue, expect the middle of this century, Global Temperature is by rising 1.5 ~ 4.5 DEG C, and coastal cities will not exist all over the world when the time comes.This problem attracts attention gradually, and has made the action of reply climate change, and people generally believe and reduce CO2 emission by global temperature rise of effectively slowing down.European Union, Japan and other countries take the lead in starting carbon emissions trading, to reduce the discharge of carbon dioxide.
In reply climate change, China has also made huge effort.First, shortly before Copenhagen climate change conference in 2009, the Chinese government has made responsible promise to the world: declined 40% ~ 45% to the GDP CO2 emission of unit of the year two thousand twenty China than 2005.Secondly, actively develop carbon emissions trading, realize reducing discharging object by the means in market.In succession reopen after a cessation of business as the pilot Beijing of carbon emission transaction in advance, Guangdong, Shanghai, Tianjin, Chongqing, Hubei and Shenzhen 7 provinces and cities, at the end of cut-off 2014, seven large pilot secondary market turnovers break through 5.3 hundred million yuan.At the beginning of 2014, national relevant ministries and commissions leader just releases the signal will run in 2016 in national carbon emissions trading market in different occasion.December 12, the Committee of Development and Reform issued " carbon emissions trading management Tentative Measures " then, and done detailed regulation to the whole process of national carbon emissions trading, so far Chinese carbon market starts to enter countdown.
In future, carbon emission power will become a kind of hard trading product.Many rows are costs, and reduction of discharging is income, how have become by carbon emission reduction additional income the problem that enterprise needs research.
Collecting carbonic anhydride and liquefaction: collecting carbonic anhydride according to technology path can be divided into burn before be separated with burn after be separated.Before burning, isolation technics is the characteristic utilizing fossil fuel to be rich in hydrocarbon two kinds of elements, the two is separated, makes the fuel based on hydrogen by chemical reaction, simultaneously separating carbon dioxide.This technology is mainly present in the preparation process of commercial syngas at present, and fossil fuel generates the synthesis gas based on hydrogen and carbon dioxide by steam reforming transformationreation, and separating-purifying obtains pure hydrogen and carbon dioxide.
After burning, isolation technics can be divided into conventional combustion and oxygen-enriched combusting again according to the difference of carbon dioxide in flue gas concentration after burning.Conventional combustion is the combustion technology that fossil fuel carries out using air as combustion adjuvant, the carbon dioxide in flue gas content that this method obtains is on the low side, general lower than 15%, follow-up pressure-swing absorption apparatus, amine aqueous solution absorption plant or the membrane separation device etc. of need being equipped with are separated purifying carbon dioxide.Burn under the oxygen-enriched combustion technology combustion adjuvant that to be fossil fuel form at pure oxygen and circulating flue gas, improved the combustion technology of the content of carbon dioxide in flue gas by flue gas recirculation, utilize the concentration of the method carbon dioxide in flue gas to reach more than 95%.
No matter be the front isolation technics of burning or the rear isolation technics of burning, the carbon dioxide obtained is all exist with gaseous state, and this gives storage, transport brings great inconvenience, and for the ease of storage, transport, the carbon dioxide trapped above needs further liquefaction.
Carbon dioxide is compressed to 2.5 ~ 3.0MPa by traditional liquefaction process, the cooling of recycling refrigeration plant and liquefaction.And utilize the cold energy of LNG, be then easy to obtain cooling and the low temperature required for liquefied carbon dioxide, thus the operating pressure of liquefying plant is down to about 0.9MPa.Compared with traditional liquefaction process, the load of refrigeration plant greatly reduces, and power consumption also reduces 30% ~ 40%.
Chinese patent 201020000778.X gives a kind of conventional coal-burning power plant collecting carbonic anhydride technology, and it utilizes ethanolamine solutions absorbing carbon dioxide, obtains separating-purifying, but this technique lacks co 2 liquefaction process, lacks the possibility of long distance transportation.
US Patent No. 7637109B2 gives a kind of oxygen-enriched combustion technology, by the control combustion temperature that adds water in a combustion chamber, produce high temperature and high pressure flue gas and promote turbine acting, flue gas separating carbon dioxide after utilizing LNG to cool acting, the program achieves the trapping of carbon dioxide, but do not consider the comprehensive utilization of energy, whole efficiency is lower.
Chinese invention patent (application number) 201310618307.3 pairs of such schemes improve, on the basis utilizing oxygen-enriched combustion technology, with the addition of the waste heat that waste heat boiler reclaims the rear flue gas of acting, utilize LNG condensing trapping carbon dioxide simultaneously, achieve on the basis of collecting carbonic anhydride, improve the total energy efficiency of device.But the program needs to increase air separation unit to prepare pure oxygen, and outfit of equipment investment is large, and unit liquid carbon dioxide cost is higher.
Chinese invention patent (application number) 02107780.0 gives the technology of LNG cold energy capturing carbon dioxide under a kind of conventional combustion.The cold energy that it utilizes LNG to gasify is sublimated the carbon dioxide in flue gas, and the carbon dioxide condensing in heat exchanger outer wall is recycled by two row parallel tube heat exchangers blocked operations, but it is larger to trap unit carbon dioxide LNG cold energy consumption in the program.
Chinese invention patent (application number) 201110073906.2 gives a kind of scheme being produced cryogenic trapping carbon dioxide by flue gas choke heat drop, the program eliminates purifying carbon dioxide process, but choke pressure is higher, air compressing expense and finishing operations are costly, and collecting carbonic anhydride rate is lower, about 10%.
Summary of the invention
The object of this invention is to provide a kind of system and device and the method thereof that utilize cold energy of liquefied natural gas trapping liquefied carbon dioxide.
System and device provided by the present invention, comprises LNG cold energy and reclaims and pressure energy recovery system, and generating and smoke circulating system and smoke carbon dioxide separating-purifying and propane cycles carbon dioxide liquefaction system three parts are reclaimed in fuel gas buring generating, fume waste heat,
Wherein, described LNG cold energy reclaims and waste heat boiler in pressure energy recovery system is denoted as that B16 generate electricity with described fuel gas buring, fume waste heat reclaims and to generate electricity and waste heat boiler in smoke circulating system is denoted as B15 and is connected;
Described LNG cold energy reclaims and heat exchanger in pressure energy recovery system is denoted as that B29 generate electricity with described fuel gas buring, fume waste heat reclaims and to generate electricity and combustion reactor in smoke circulating system is denoted as B13 and is connected;
Described smoke carbon dioxide separating-purifying and propane cycles carbon dioxide liquefaction system are reclaimed with described LNG cold energy respectively by waste heat boiler B16 and pressure energy recovery system generates electricity with described fuel gas buring, fume waste heat reclaims and to generate electricity and waste heat boiler B15 in smoke circulating system is connected.
In said system device, described LNG cold energy reclaims and pressure energy recovery system comprises that LNG high-pressure pump is denoted as B24, heat exchanger is denoted as B25, condenser is denoted as B26, current divider is denoted as B27, waste heat boiler B16, combustion gas turbine are denoted as B28 and heat exchanger B29; Described LNG high-pressure pump B24, heat exchanger B25, condenser B26, current divider B27, waste heat boiler B16, combustion gas turbine B28 are connected successively with heat exchanger B29.
The generating of described fuel gas buring, fume waste heat are reclaimed generating and smoke circulating system and are comprised that flue gas air mixer is denoted as B11, air compressor is denoted as B12, combustion reactor B13, smoke gas turbine are denoted as B14 and steam Lang Ken cycle generating system; Described flue gas air mixer B11, air compressor B12, combustion reactor B13, smoke gas turbine B14 are connected successively with steam Lang Ken cycle generating system,
It is wherein, described that steam Lang Ken cycle generating system comprises waste heat boiler B15, high-pressure steam turbine is denoted as B20, middle pressure steam turbine is denoted as B21, condenser is denoted as B22 and water circulating pump is denoted as B23; Described waste heat boiler B15, high-pressure steam turbine B20, middle pressure steam turbine B21, condenser B22 are connected successively with water circulating pump B23.
In described smoke carbon dioxide separating-purifying and propane cycles carbon dioxide liquefaction system, smoke carbon dioxide system for separating and purifying comprises waste heat boiler B16, cooler is denoted as B17, gas-liquid separator is denoted as B18, current divider is denoted as B19, compressor is denoted as B30, heat exchanger is denoted as B31, molecular sieve dehydrater is denoted as B32 and CO
2purifying system is denoted as B33; Described waste heat boiler B16, cooler B17, gas-liquid separator B18, current divider B19, compressor B30, heat exchanger B31, molecular sieve dehydrater B32 and CO
2purifying system B33 connects successively,
Wherein, in described smoke carbon dioxide separating-purifying and propane cycles carbon dioxide liquefaction system, propane cycles carbon dioxide liquefaction system comprises CO
2liquefier is denoted as B36, propane cycles pump is denoted as B37 and heat exchanger is denoted as B25; Described CO
2liquefier B36, propane cycles pump B37 are connected successively with heat exchanger B25.
Method provided by the present invention, comprises the steps:
1) air and circulating flue gas are denoted as F-GAS16 and are mixed to get gaseous mixture, and gaseous mixture is denoted as NG7 again and mixes, burns with natural gas, generate flue gas and are denoted as F-GAS1, and flue gas F-GAS1 enters turbine acting, and the flue gas after acting is denoted as F-GAS2;
Flue gas F-GAS2 enters the boiler of the steam Lang Ken circulatory system, and recirculated water in the boiler steam raising obtains steam and is denoted as STEAM-1, and steam STEAM-1 is done work by turbine, and the steam after acting is denoted as STEAM-2; Steam STEAM-2 enters the boiler heating of the steam Lang Ken circulatory system again, obtains steam and is denoted as STEAM-3, and steam STEAM-3 is done work by turbine, and the steam after acting is denoted as STEAM-4; Steam STEAM-4 is all condensed into aqueous water and again circulates through circulating pump pressurization; The flue gas of discharging from the steam Lang Ken circulatory system is denoted as F-GAS3;
Flue gas F-GAS3 and natural gas are denoted as NG4 and carry out heat exchange, and the natural gas after heat exchange is denoted as NG5, and the flue gas after heat exchange is denoted as F-GAS4;
2) liquefied natural gas is through pressurization and propane heat exchange, and the propane temperature after heat exchange reduces, and LNG temperature raises, and gasifies as high-pressure natural gas, is denoted as NG1;
High-pressure natural gas NG1 enters distributing system through final temperature adjustment, and the high-pressure natural gas entering 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 directly enters urban pipe network;
NG4 and flue gas F-GAS3 carries out heat exchange, and the flue gas after heat exchange is denoted as F-GAS4, and the natural gas after heat exchange is denoted as NG5, and natural gas NG5 is done work by turbine; Natural gas via temperature adjustment after acting mixes with circulating flue gas and air, burns.
3) flue gas F-GAS4 is cooled to normal temperature through condenser, and cooled flue gas is denoted as F-GAS5;
Flue gas F-GAS5 is through gas-liquid separator, and remove condensed water, the flue gas obtained is denoted as F-GAS6; Flue gas F-GAS6 is divided into two strands, one be used as circulating flue gas, with air and natural gas mixed combustion, another stock is for reclaiming carbon dioxide; Flue gas for reclaiming carbon dioxide is denoted as F-GAS7;
Flue gas F-GAS7 once boosts through compressor and obtains flue gas and be denoted as F-GAS8, and through water quench, the molecular sieve degree of depth dewaters and obtains pure flue gas F-GAS10;
Flue gas F-GAS10 enters Pressure Swing Adsorption system (comprising absorption and desorption) and obtains rich carbonated flue 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 reduces, and obtains flue gas F-GAS14 and the step 1 of cold) propane heat exchange in propane cycles, the co 2 liquefaction in flue gas, is denoted as L-CO2;
In said method, step 1) in, the volume ratio of described air and circulating flue gas F-GAS16 is 10:(5 ~ 7).
The temperature of described flue gas F-GAS1 is 1200 ~ 1350 DEG C.
The temperature of described flue gas F-GAS2 is 550 ~ 700 DEG C, and pressure is 1.1 ~ 1.5atm.
The temperature of described flue gas F-GAS13 is 20 ~ 35 DEG C, and pressure is 8 ~ 9atm.Described flue gas F-GAS6 is divided into two strands, and the volume ratio of described circulating flue gas and flue gas F-GAS7 is 1:(1 ~ 2).
In said method, step 2) in, described propane is through the pressurization of propane cycles pump, and pressure raises, and is denoted as C
3h
8-1; Propane after pressurization enters heat exchanger and LNG heat-exchange temperature reduces, and is denoted as C
3h
8-2, propane and step 3 that temperature reduces) the middle final heat-exchange temperature of F-GAS14 raises, and is denoted as C
3h
8-3; Propane C
3h
8-3 enter propane cycles pump has again pressurizeed whole circulation.The temperature of the propane C3H8-2 after described heat exchange is-70 ~-50 DEG C.
The present invention utilizes the cold energy discharged during liquefied natural gas gasifying to carry out liquefied carbon dioxide, and has incorporated plant gas and cold energy of liquefied natural gas generates electricity.The program improves carbon dioxide in flue gas concentration by part of smoke circulation, reduce the investment cost of carbon dioxide in flue gas purifier, LNG cold energy is utilized to provide low temperature, reduce investment and the operating cost of carbon dioxide liquid gasifying device, utilize the UTILIZATION OF VESIDUAL HEAT IN of flue gas to improve the generating efficiency of LNG cold energy simultaneously.The program can be used for the cold energy use planning of newly-built LNG receiving station, also may be used for the plant gas transformation relying on LNG receiving station to build.
Compared with prior art, the present invention has following beneficial effect:
1) the present invention adopts air to cook combustion adjuvant, without the need to pure oxygen, eliminates air separation unit.
2) achieve the variation of LNG cold energy to utilize: in the last few years, cold energy of liquefied natural gas utilizes technology to obtain the attention of people gradually, China sea oil has built up domestic first set LNG cold energy air separation unit at Putian, fujian Province, but LNG cold energy collecting carbonic anhydride technology is still in theory and technology conceptual phase, and unrealized industrialization, herein by LNG cold energy use and CO
2liquefaction trapping combines the recovery not only realizing LNG cold energy, and reduces liquid carbon dioxide production cost, achieves the efficient variation of LNG cold energy and utilizes.
3) cold transmits safety: pass through LNG-propane heat exchanger in cold transfer stages herein, achieve LNG cold to CO
2the safe transfer of liquefaction unit, simultaneously, the introducing of refrigerant propane adds CO
2the operating flexibility of liquefaction unit, avoids the risk of carbon dioxide because of low temperature frozen plug pipeline.
4) equipment operating expense is low: the carbon dioxide in flue gas concentration of conventional gas turbines is lower, this programme adopts the scheme of partial fume circulation to add the concentration of carbon dioxide in flue gas, and this reduces follow-up flue gas treating process cost of equipment and finishing operations expense to a certain extent.
5) system effectiveness is high: this programme is by gas turbine power generation, and LNG cold energy use, co 2 liquefaction, NG pressure energy utilizes and integrates the efficiency utilization achieving energy efficiency, and entire system efficiency reaches 45.7%.
Accompanying drawing explanation
Fig. 1 is the process chart of cold energy of liquefied natural gas trapping liquefaction plant gas carbon dioxide in embodiment 1, wherein, and B11-air flue gas blender; B12-air compressor; B13-combustion reactor; B14-smoke gas turbine; B15-waste heat boiler; B16-waste heat boiler; B17-cooler; B18-gas-liquid separator; B19-current divider; B20-high-pressure steam turbine; B21-middle pressure steam turbine; B22-cooler; B23-water circulating pump; B24-LNG pump; B25-heat exchanger; B26-condenser; B27-current divider; B28-combustion gas turbine; B29-heat exchanger; B30-compressor; B31-heat exchanger; B32-molecular sieve dehydrater; B33-CO
2purifying system; B34-compressor; B35-condenser; B36-CO
2liquefier; B37-propane cycles pump.
Detailed description of the invention
Below by specific embodiment, method of the present invention is described, but the present invention is not limited thereto.
Experimental technique described in following embodiment, if no special instructions, is conventional method; Described reagent and material, if no special instructions, all can obtain from commercial channels.
In following embodiment, the isentropic efficiency of compressor, combustion gas turbine, flue gas turbine expander turbine, steam turbine gets 0.9, and mechanical efficiency gets 0.95, and the efficiency of pump gets 0.95, and mechanical efficiency gets 0.9, and scheme puts aside device Pressure Drop.
In following embodiment, 1atm, the cold fire of LNG of-161 DEG C are with being 402.3KJ/Kg.
In following embodiment, methane Lower heat value 35.99MJ/Nm
3.
In following embodiment, formula used is as follows:
Generating efficiency=net power output/(gas consumption X natural gas status calorific value)
Overall efficiency=net power output/(gas consumption X natural gas status calorific value+LNG measures the cold fire of XLNG unit and uses)
Embodiment 1, the method utilizing liquefied natural gas (LNG) cold energy capturing carbon dioxide and system thereof:
One, the system of cold energy of liquefied natural gas capturing carbon dioxide is utilized, its system architecture is as shown in Figure 1: comprise LNG cold energy and reclaim and pressure energy recovery system, and generating (vapor recycle electricity generation system) and smoke circulating system and smoke carbon dioxide separating-purifying and propane cycles carbon dioxide liquefaction system three parts are reclaimed in fuel gas buring generating, fume waste heat.
Wherein, described LNG cold energy reclaims and pressure energy recovery system comprises LNG high-pressure pump B24, heat exchanger B25, condenser is denoted as B26, current divider B27, waste heat boiler B16, combustion gas turbine B28 and heat exchanger B29; Described LNG high-pressure pump 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 turbine) are connected successively with heat exchanger B29.
Described fuel gas buring generating, fume waste heat recovery generating (vapor recycle electricity generation system) and smoke circulating system comprise flue gas air mixer B11, air compressor B12, combustion reactor B13, smoke gas turbine B14 and steam Lang Ken cycle generating system; Described flue gas air mixer B11, air compressor B12, combustion reactor B13, smoke gas turbine B14 are connected successively with steam Lang Ken cycle generating system.
Wherein, described steam Lang Ken cycle generating system comprises waste heat boiler B15, high-pressure steam turbine B20, middle pressure steam turbine B21, condenser B22 and water circulating pump B23; Described waste heat boiler B15, high-pressure steam turbine B20, middle pressure steam turbine B21, condenser B22 are connected successively with water circulating pump B23.
In described smoke carbon dioxide separating-purifying and propane cycles carbon dioxide liquefaction system, smoke carbon dioxide system for separating and purifying comprises waste heat boiler B16, cooler B17, gas-liquid separator B18, current divider B19, compressor B30, heat exchanger B31, molecular sieve dehydrater B32 and CO
2purifying system B33; Described waste heat boiler B16, cooler B17, gas-liquid separator B18, current divider B19, compressor B30, heat exchanger B31, molecular sieve dehydrater B32 and CO
2purifying system B33 connects successively.
Wherein, in described smoke carbon dioxide separating-purifying and propane cycles carbon dioxide liquefaction system, propane cycles carbon dioxide liquefaction system comprises CO
2liquefier B36, propane cycles pump B37 and heat exchanger B25; Described CO
2liquefier B36, propane cycles pump B37 are connected successively with heat exchanger B25.
Two, utilize the method for liquefied natural gas (LNG) cold energy capturing carbon dioxide, process chart as shown in Figure 1:
1) plant gas generating: under the status of criterion 500,000Nm
3the air (AIR) of/h with from step 2) 330,000Nm
3the circulating flue gas F-GAS16 of/h mixes in air flue gas blender B11, boosts to 13 ~ 20atm, specifically boost to 17atm through air compressor B12.
Come from the 25000Kg/h of LNG gasification section, 30 DEG C, the natural gas NG7 of 17bar and gaseous mixture are denoted as F-GAS18 and enter in combustion reactor B13 generation 1280 DEG C of burning, the high temperature and high pressure flue gas F-GAS1 of 17bar, high temperature and high pressure flue gas promotes smoke gas turbine B14 acting, temperature is down to 630 DEG C, and Pressure Drop is to 1.3atm.
Above-mentioned steps is conventional gas power plants generating electricity technique, and smoke gas turbine B14 and air compressor B12 coaxially does work, and total generated output is 119.3MW.
The flue gas F-GAS2 discharged from smoke gas turbine B14 enters the steam Lang Ken circulatory system, reclaims its remaining heat.Concrete steps are as follows:
After acting, flue gas F-GAS2 temperature is 630 DEG C, from the 240t/h of water circulating pump B23 (i.e. boiler feed pump), 18MPa, the recirculated water of 105 DEG C in waste heat boiler (B15) with flue gas heat exchange, through heat exchange, evaporation, overheated, recirculated water produces 580 DEG C in waste heat boiler B15, and 18MPa superheated steam STEAM-1, flue gas F-GAS2 temperature is down to about 110 DEG C.High steam STEAM-1 enters in high-pressure steam turbine B20 and does work, and the pressure flowed out from steam turbine is 7MPa, and temperature is down to 350 DEG C for its temperature.Then again absorb heat being sent back in waste heat boiler B15 by steam STEAM-2, temperature rises to 530 DEG C.Steam STEAM-3 is delivered to middle pressure steam turbine B21 to do work, temperature drops to 120 DEG C, and pressure drop is to 1.2atm.Through cooler B22 (i.e. cooling tower) cooling, steam STEAM-4 is all condensed into aqueous water, and aqueous water through water circulating pump B23 supercharging, is delivered in waste heat boiler B15 and recycles again.
This step completes a complete steam Lang Ken and circulates, and clean generated output is 65.7MW.
2) LNG cold energy reclaims and pressure energy generating:
LNG is stored in LNG storage tank with normal pressure (1atm) state, and temperature is-161 DEG C.For reaching transmission & distribution requirement, need LNG to be forced into ductwork pressure.
From storage tank 30t/h LNG be forced into 8MPa through pump B24, enter heat exchanger B25 and step 3) in propane (C3H8-1) heat exchange of 500t/h.LNG gasification is high-pressure gas in this step, and propane temperature is down to-65 DEG C.In order to improve capacity usage ratio further, high-pressure gas and step 3) in the high-pressure carbon dioxide heat exchange of purification, temperature rises to zero degree, and carbon dioxide is cooled to-30 DEG C.After this step, combustion gas enters the remote transmission & distribution of distributing system through last temperature adjustment.
The 8MPa natural gas NG2 entering distributing system isolates two strands at current divider B27 place, and one natural gas NG3 directly enters urban pipe network, and the natural gas NG4 of another gang of 7Kg/s is used for gas turbine combustion.The operating pressure of gas turbine is 17atm, just can enter in the B13 of combustion reaction room and burn after this gang of natural gas NG4 needs pressure regulation.In order to improve generating efficiency and follow-up gas turbine combustion efficiency, this gang of natural gas NG4 again with step 1) in waste heat boiler B16, carry out secondary heat exchange raised temperature to 95 DEG C close to the flue gas F-GAS3 of normal pressure, combustion gas NG5 is passed into combustion gas turbine B28 expansion work, after Pressure Drop to 17atm, enter into combustion reactor (gas-turbine combustion chamber) combustion power generation.
This step is that gaseous-pressure can reclaim, and clean 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, the flue gas F-GAS4 temperature of discharging from waste heat boiler B16 is connected to nearly 105 DEG C, normal temperature is cooled to through cooler B17, most of steam liquefaction in flue gas, by flue gas F-GAS5 by gas-liquid separator B18 removing condensed water wherein, obtain flue gas F-GAS6, this flue gas consists of nitrogen 83%, oxygen 5%, carbon dioxide 10%.
By flue gas F-GAS6 by current divider B19 by volume 1:1 be divided into two strands, one is for step 1) in air mixing, for circulating combustion, another stock be used for collecting carbonic anhydride.
330,000Nm is separated through current divider B19
3the flue gas F-GAS7 of/h is for reclaiming carbon dioxide, flue gas F-GAS7 is by being forced into 4atm in compressor B30, at compressor outlet, cooler B31 cooled flue gas is set to normal temperature, flue gas F-GAS9 to dewater the pure flue gas obtained based on nitrogen, oxygen, carbon dioxide through the molecular sieve dehydrater B32 degree of depth, then by it through CO
2the process of purifying system B33 (Pressure Swing Adsorption workshop section comprises the techniques such as adsorption and desorption), obtains the carbon dioxide of purity more than 95% (i.e. flue gas F-GAS11), the rate of recovery 85% of this step 2 carbonoxide.
Flue gas F-GAS11 is pressurized to 9atm through compressor B34, and arrange condenser at compressor end and be denoted as B35 cooled flue 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 CO
2liquefy in liquefier B36, remove residual nitrogen and oxygen etc., obtain liquefied carbon dioxide (L-CO
2), temperature-50 DEG C, purity 98%, the rate of recovery 95% of this step 2 carbonoxide.
Liquid carbon dioxide can through the follow-up deep processing process of refinement of row as required.
In upper step, co 2 liquefaction process workshop section comprises the cyclic process that take propane as refrigerant.The propane of 500t/h is forced into 3atm through propane cycles pump B37, and enter LNG-propane heat exchanger B25 and LNG heat exchange, temperature is down to-65 DEG C, and the propane obtaining cold enters CO
2be denoted as F-GAS14 heat exchange with the carbon dioxide being chilled to-30 DEG C in advance in liquefier B36, the liquefaction of carbon dioxide absorption cold is liquid carbon dioxide (L-CO
2), temperature is-50 DEG C, and propane pressurizes through propane cycles pump B37, again enters in LNG-propane heat exchanger and completes whole circulation.
According to above-mentioned technique, after the power consumption 24WM of deduction compressor and pump, system net power output is 162.5WM.According to generating efficiency and comprehensive energy efficiency formula, the calculating comprehensive utilization cold energy of liquefied natural gas trapping method of liquefied carbon dioxide and the generating efficiency of system thereof are 46.2%, and comprehensive energy efficiency is 45.7%, recovery rate of CO 2 81%.
Claims (7)
1. the system and device utilizing cold energy of liquefied natural gas to trap liquefied carbon dioxide, comprise LNG cold energy to reclaim and pressure energy recovery system, generating and smoke circulating system and smoke carbon dioxide separating-purifying and propane cycles carbon dioxide liquefaction system three parts are reclaimed in fuel gas buring generating, fume waste heat;
Wherein, described LNG cold energy reclaims and waste heat boiler B16 in pressure energy recovery system generate electricity with described fuel gas buring, fume waste heat reclaims and to generate electricity and waste heat boiler B15 in smoke circulating system is connected;
Described LNG cold energy reclaims and heat exchanger B29 in pressure energy recovery system generate electricity with described fuel gas buring, fume waste heat reclaims and to generate electricity and combustion reactor B13 in smoke circulating system is connected;
Described smoke carbon dioxide separating-purifying and propane cycles carbon dioxide liquefaction system are reclaimed with described LNG cold energy respectively by waste heat boiler B16 and pressure energy recovery system generates electricity with described fuel gas buring, fume waste heat reclaims and to generate electricity and waste heat boiler B15 in smoke circulating system is connected.
2. system and device according to claim 1, is characterized in that: described LNG cold energy reclaims and pressure energy recovery system comprises that LNG high-pressure pump is denoted as B24, heat exchanger is denoted as B25, condenser is denoted as B26, current divider is denoted as B27, waste heat boiler is denoted as B16, combustion gas turbine is denoted as B28 and heat exchanger is denoted as B29; Described LNG high-pressure pump B24, heat exchanger B25, condenser B26, current divider B27, waste heat boiler B16, combustion gas turbine B28 are connected successively with heat exchanger B29.
3. system and device according to claim 1 and 2, is characterized in that: the generating of described fuel gas buring, fume waste heat are reclaimed generating and smoke circulating system and comprised that flue gas air mixer is denoted as B11, air compressor is denoted as B12, combustion reactor is denoted as B13, smoke gas turbine is denoted as B14 and steam Lang Ken cycle generating system; Described flue gas air mixer B11, air compressor B12, combustion reactor B13, smoke gas turbine B14 are connected successively with steam Lang Ken cycle generating system;
Wherein, described steam Lang Ken cycle generating system comprises that waste heat boiler is denoted as B15, high-pressure steam turbine is denoted as B20, middle pressure steam turbine is denoted as B21, condenser is denoted as B22 and water circulating pump is denoted as B23; Described waste heat boiler B15, high-pressure steam turbine B20, middle pressure steam turbine B21, condenser B22 are connected successively with water circulating pump B23.
4. the system and device according to any one of claim 1-3, is characterized in that: in described smoke carbon dioxide separating-purifying and propane cycles carbon dioxide liquefaction system, smoke carbon dioxide system for separating and purifying comprises that waste heat boiler is denoted as B16, cooler is denoted as B17, gas-liquid separator is denoted as B18, current divider is denoted as B19, compressor is denoted as B30, heat exchanger is denoted as B31, molecular sieve dehydrater is denoted as B32 and CO
2purifying system is denoted as B33; Described waste heat boiler B16, cooler B17, gas-liquid separator B18, current divider B19, compressor B30, heat exchanger B31, molecular sieve dehydrater B32 and CO
2purifying system B33 connects successively;
In described smoke carbon dioxide separating-purifying and propane cycles carbon dioxide liquefaction system, propane cycles carbon dioxide liquefaction system comprises CO
2liquefier is denoted as B36, propane cycles pump is denoted as B37 and heat exchanger is denoted as B25; Described CO
2liquefier B36, propane cycles pump B37 are connected successively with heat exchanger B25.
5. utilize the method for the system and device capturing carbon dioxide according to any one of claim 1-4, comprise the steps:
1) air and circulating flue gas are denoted as F-GAS16 and are mixed to get gaseous mixture, and gaseous mixture is denoted as NG7 again and mixes, burns with natural gas, generate flue gas and are denoted as F-GAS1, and flue gas F-GAS1 enters turbine acting, and the flue gas after acting is denoted as F-GAS2;
Flue gas F-GAS2 enters the boiler of the steam Lang Ken circulatory system, and recirculated water in the boiler steam raising obtains steam and is denoted as STEAM-1, and steam STEAM-1 is done work by turbine, and the steam after acting is denoted as STEAM-2; Steam STEAM-2 enters the boiler heating of the steam Lang Ken circulatory system again, obtains steam and is denoted as STEAM-3, and steam STEAM-3 is done work by turbine, and the steam after acting is denoted as STEAM-4; Steam STEAM-4 is all condensed into aqueous water and again circulates through circulating pump pressurization; The flue gas of discharging from the steam Lang Ken circulatory system is denoted as F-GAS3;
Flue gas F-GAS3 and natural gas are denoted as NG4 and carry out heat exchange, and the natural gas after heat exchange is denoted as NG5, and the flue gas after heat exchange is denoted as F-GAS4;
2) liquefied natural gas is through pressurization and propane heat exchange, and the propane temperature after heat exchange reduces, and LNG temperature raises, and gasifies as high-pressure natural gas, is denoted as NG1;
High-pressure natural gas NG1 enters distributing system through final temperature adjustment, and the high-pressure natural gas entering 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 directly enters urban pipe network;
NG4 and flue gas F-GAS3 carries out heat exchange, and the flue gas after heat exchange is denoted as F-GAS4, and the natural gas after heat exchange is denoted as NG5, and natural gas NG5 is done work by turbine; Natural gas via temperature adjustment after acting mixes with circulating flue gas and air, burns;
3) flue gas F-GAS4 is cooled to normal temperature through condenser, and cooled flue gas is denoted as F-GAS5;
Flue gas F-GAS5 is through gas-liquid separator, and remove condensed water, the flue gas obtained is denoted as F-GAS6; Flue gas F-GAS6 is divided into two strands, one be used as circulating flue gas, with air and natural gas mixed combustion, another stock is for reclaiming carbon dioxide; Flue gas for reclaiming carbon dioxide is denoted as F-GAS7;
Flue gas F-GAS7 once boosts through compressor and obtains flue gas and be denoted as F-GAS8, and through water quench, the molecular sieve degree of depth dewaters and obtains pure flue gas F-GAS10;
Flue gas F-GAS10 enters Pressure Swing Adsorption system and obtains rich carbonated flue 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 reduces, and obtains flue gas F-GAS14 and the step 1 of cold) propane heat exchange in propane cycles, the co 2 liquefaction in flue gas, is denoted as L-CO2.
6. method according to claim 5, is characterized in that: step 1) in, the volume ratio of described air and circulating flue gas F-GAS16 is 10:(5 ~ 7);
The temperature of described flue gas F-GAS1 is 1200 ~ 1350 DEG C;
The temperature of described flue gas F-GAS2 is 550 ~ 700 DEG C, and pressure is 1.1 ~ 1.5atm;
The temperature of described flue gas F-GAS13 is 20 ~ 35 DEG C, and pressure is 8 ~ 9atm;
Described flue gas F-GAS6 is divided into two strands, and the volume ratio of described circulating flue gas and flue gas F-GAS7 is 1:(1 ~ 2).
7. the method according to claim 5 or 6, is characterized in that: step 2) in, described propane is through the pressurization of propane cycles pump, and pressure raises, and is denoted as C
3h
8-1; Propane after pressurization enters heat exchanger and LNG heat-exchange temperature reduces, and is denoted as C
3h
8-2, propane and step 3 that temperature reduces) the middle final heat-exchange temperature of F-GAS14 raises, and is denoted as C
3h
8-3; Propane C
3h
8-3 enter propane cycles pump has again pressurizeed whole circulation.The temperature of the propane C3H8-2 after described heat exchange is-70 ~-50 DEG C;
Propane C after described heat exchange
3h
8the temperature of-2 is-70 ~-50 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510490793.4A CN105115245B (en) | 2015-08-11 | 2015-08-11 | The system and device and its method of liquefied carbon dioxide are trapped using cold energy of liquefied natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510490793.4A CN105115245B (en) | 2015-08-11 | 2015-08-11 | The system and device and its method of liquefied carbon dioxide are trapped using cold energy of liquefied natural gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105115245A true CN105115245A (en) | 2015-12-02 |
| CN105115245B CN105115245B (en) | 2017-07-11 |
Family
ID=54663292
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510490793.4A Active CN105115245B (en) | 2015-08-11 | 2015-08-11 | The system and device and its method of liquefied carbon dioxide are trapped using cold energy of liquefied natural gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105115245B (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109281719A (en) * | 2017-07-20 | 2019-01-29 | 斗山重工业建设有限公司 | Hybrid power system |
| CN109838684A (en) * | 2019-01-25 | 2019-06-04 | 集美大学 | The use of underwater boat device exhaust gas and storage device and its method |
| CN113738467A (en) * | 2021-09-23 | 2021-12-03 | 浙江浙能温州液化天然气有限公司 | Integrated system for carbon-carrying capture power generation by utilizing liquefied natural gas |
| CN113959178A (en) * | 2021-11-29 | 2022-01-21 | 李欣锐 | Carbon capture method in hydrogen production process by LNG |
| CN114263511A (en) * | 2021-12-21 | 2022-04-01 | 西安石油大学 | Light hydrocarbon separation coupling parallel backheating organic Rankine cycle power generation system utilizing LNG cold energy |
| CN114961899A (en) * | 2022-05-12 | 2022-08-30 | 江苏科技大学 | LNG power ship waste heat and cold energy comprehensive utilization system with carbon capture function |
| CN115301045A (en) * | 2022-08-03 | 2022-11-08 | 安徽省生态环境科学研究院 | Carbon source trapping and storing integrated equipment |
| CN116335823A (en) * | 2022-11-24 | 2023-06-27 | 浙江大学 | Combined cycle system combined with Allam cycle type power station and low-temperature cycle method |
| CN118703335A (en) * | 2024-08-28 | 2024-09-27 | 天津大学 | Liquid collection, preparation method and application thereof in fuel oil |
| CN118703335B (en) * | 2024-08-28 | 2024-11-19 | 天津大学 | Liquid collection, preparation method and application thereof in fuel oil |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1190449A (en) * | 1995-06-01 | 1998-08-12 | 卡伯特公司 | Liquefied natural gas (LNG) fueled combined cycle power plant and LNG fueled gas turbine plant |
| CN1737351A (en) * | 2005-09-01 | 2006-02-22 | 西安交通大学 | System and method for improving efficiency of combined cycle electric power plant |
| CN102628402A (en) * | 2012-04-17 | 2012-08-08 | 西安交通大学 | Fuel cell and organic Rankine cycle combined power generating system based on LNG (Liquefied Natural Gas) cold energy utilization |
| CN103628982A (en) * | 2013-11-27 | 2014-03-12 | 暨南大学 | Combined power circulating method capable of catching carbon dioxide (CO2) by using LNG (Liquefied Natural Gas) cold energy and system thereof |
| 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 |
| WO2014127913A2 (en) * | 2013-02-21 | 2014-08-28 | Faramarz Bairamijamal | High pressure process for co2 capture, utilization for heat recovery, power cycle, super-efficient hydrogen based fossil power generation and conversion of liquid co2 with water to syngas and oxygen |
-
2015
- 2015-08-11 CN CN201510490793.4A patent/CN105115245B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1190449A (en) * | 1995-06-01 | 1998-08-12 | 卡伯特公司 | Liquefied natural gas (LNG) fueled combined cycle power plant and LNG fueled gas turbine plant |
| CN1737351A (en) * | 2005-09-01 | 2006-02-22 | 西安交通大学 | System and method for improving efficiency of combined cycle electric power plant |
| CN102628402A (en) * | 2012-04-17 | 2012-08-08 | 西安交通大学 | Fuel cell and organic Rankine cycle combined power generating system based on LNG (Liquefied Natural Gas) cold energy utilization |
| WO2014127913A2 (en) * | 2013-02-21 | 2014-08-28 | Faramarz Bairamijamal | High pressure process for co2 capture, utilization for heat recovery, power cycle, super-efficient hydrogen based fossil power generation and conversion of liquid co2 with water to syngas and oxygen |
| CN103628982A (en) * | 2013-11-27 | 2014-03-12 | 暨南大学 | Combined power circulating method capable of catching carbon dioxide (CO2) by using LNG (Liquefied Natural Gas) cold energy and system thereof |
| 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 |
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109281719A (en) * | 2017-07-20 | 2019-01-29 | 斗山重工业建设有限公司 | Hybrid power system |
| CN109281719B (en) * | 2017-07-20 | 2021-05-14 | 斗山重工业建设有限公司 | Hybrid power generation system |
| CN109838684A (en) * | 2019-01-25 | 2019-06-04 | 集美大学 | The use of underwater boat device exhaust gas and storage device and its method |
| CN113738467A (en) * | 2021-09-23 | 2021-12-03 | 浙江浙能温州液化天然气有限公司 | Integrated system for carbon-carrying capture power generation by utilizing liquefied natural gas |
| CN113738467B (en) * | 2021-09-23 | 2023-07-14 | 浙江浙能温州液化天然气有限公司 | Integrated system for carrying out carbon-carrying capturing power generation by utilizing liquefied natural gas |
| CN113959178B (en) * | 2021-11-29 | 2023-01-20 | 李欣锐 | Carbon capture method in hydrogen production process by LNG |
| CN113959178A (en) * | 2021-11-29 | 2022-01-21 | 李欣锐 | Carbon capture method in hydrogen production process by LNG |
| CN114263511A (en) * | 2021-12-21 | 2022-04-01 | 西安石油大学 | Light hydrocarbon separation coupling parallel backheating organic Rankine cycle power generation system utilizing LNG cold energy |
| CN114263511B (en) * | 2021-12-21 | 2024-01-26 | 西安石油大学 | Light hydrocarbon separation coupling parallel backheating organic Rankine cycle power generation system utilizing LNG cold energy |
| CN114961899A (en) * | 2022-05-12 | 2022-08-30 | 江苏科技大学 | LNG power ship waste heat and cold energy comprehensive utilization system with carbon capture function |
| CN114961899B (en) * | 2022-05-12 | 2024-07-16 | 江苏科技大学 | LNG power ship waste heat and cold energy comprehensive utilization system with carbon capture function |
| CN115301045A (en) * | 2022-08-03 | 2022-11-08 | 安徽省生态环境科学研究院 | Carbon source trapping and storing integrated equipment |
| CN115301045B (en) * | 2022-08-03 | 2023-05-16 | 安徽省生态环境科学研究院 | Integrative equipment is stored in carbon source entrapment |
| CN116335823A (en) * | 2022-11-24 | 2023-06-27 | 浙江大学 | Combined cycle system combined with Allam cycle type power station and low-temperature cycle method |
| CN116335823B (en) * | 2022-11-24 | 2024-01-23 | 浙江大学 | Combined cycle system combined with Allam cycle type power station and low-temperature cycle method |
| CN118703335A (en) * | 2024-08-28 | 2024-09-27 | 天津大学 | Liquid collection, preparation method and application thereof in fuel oil |
| CN118703335B (en) * | 2024-08-28 | 2024-11-19 | 天津大学 | Liquid collection, preparation method and application thereof in fuel oil |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105115245B (en) | 2017-07-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105115245B (en) | The system and device and its method of liquefied carbon dioxide are trapped using cold energy of liquefied natural gas | |
| CN103075250B (en) | Method for generating by graded use of cold energy of liquefied natural gas | |
| CN100470114C (en) | Carbon dioxide zero discharge thermodynamic cycle and procedure using liquefied natural gas cool | |
| CN103628982B (en) | Utilize combined power circulation method and the system thereof of cold energy of liquefied natural gas capturing carbon dioxide | |
| CN102061950B (en) | Device for capturing CO2 from flue gas by ultralow temperature generation joint cryogenic medium-pressure method | |
| CN203906025U (en) | Island energy supply system | |
| CN101922352A (en) | Thermal circulation system cooled by liquefied natural gas and flow | |
| CN103993920A (en) | Island energy supply system with cold energy | |
| CN108661732A (en) | A kind of liquefied natural gas (LNG) production system of combustion gas-supercritical carbon dioxide combined power | |
| CN108795508B (en) | Method for separating coke oven gas by utilizing expansion refrigeration of nitrogen and helium | |
| CN113738467B (en) | Integrated system for carrying out carbon-carrying capturing power generation by utilizing liquefied natural gas | |
| CN104266454A (en) | Liquefied natural gas production system with gas-supercritical carbon dioxide united power | |
| CN101566104B (en) | Method and device for zero emission of carbon dioxide by utilizing liquid hydrogen condensation | |
| CN201104074Y (en) | Skid mounted biogas purifying and liquefying device | |
| CN113882955A (en) | Gas turbine reheating combined cycle power generation system and operation method thereof | |
| CN115750009B (en) | Energy storage power peak regulation system for carbon capture and liquefied natural gas cold energy utilization and operation method | |
| CN101318620A (en) | Chemical industry power multi-generation energy resource system and method for separating C02 | |
| CN114961899B (en) | LNG power ship waste heat and cold energy comprehensive utilization system with carbon capture function | |
| CN114046172B (en) | System and method for treating and utilizing coal fire based on carbon dioxide process and modularized design | |
| CN115199367A (en) | Power generation system and method based on coupling zero-energy-consumption carbon dioxide capture of chemical reinjection natural gas reforming gas turbine | |
| CN110529208B (en) | LNG cold energy cascade utilization control system and control method | |
| CN110185506B (en) | Pressure energy comprehensive utilization system of natural gas pressure regulating station | |
| CN109282575B (en) | Follow-on hydrogen mixed working medium waste heat utilization system | |
| CN216665760U (en) | Gas turbine-ORC combined cycle and intake air cooling power generation system and device | |
| CN114017993B (en) | Device and method for producing hydrogen and byproduct oxygen by utilizing green electrolysis water |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
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. |
|
| TR01 | Transfer of patent right |