CN1447016A - Gas turbine generating system and flow by cooling liquefied natural gas to separate carbon dioxide - Google Patents
Gas turbine generating system and flow by cooling liquefied natural gas to separate carbon dioxide Download PDFInfo
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- 239000003949 liquefied natural gas Substances 0.000 title claims abstract description 179
- 239000007789 gas Substances 0.000 title claims abstract description 147
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims description 39
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims description 18
- 238000001816 cooling Methods 0.000 title claims description 18
- 239000001569 carbon dioxide Substances 0.000 title claims description 17
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 84
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 70
- 238000000034 method Methods 0.000 claims abstract description 48
- 238000002485 combustion reaction Methods 0.000 claims abstract description 43
- 239000003345 natural gas Substances 0.000 claims abstract description 40
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 34
- 239000006200 vaporizer Substances 0.000 claims abstract description 31
- 230000008569 process Effects 0.000 claims abstract description 28
- 238000010248 power generation Methods 0.000 claims abstract description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 23
- 239000007787 solid Substances 0.000 claims abstract description 14
- 239000000446 fuel Substances 0.000 claims abstract description 11
- 238000002309 gasification Methods 0.000 claims description 29
- 238000010438 heat treatment Methods 0.000 claims description 20
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 16
- 239000001301 oxygen Substances 0.000 claims description 16
- 229910052760 oxygen Inorganic materials 0.000 claims description 16
- 239000000203 mixture Substances 0.000 claims description 5
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 4
- 239000012530 fluid Substances 0.000 claims description 3
- 238000003860 storage Methods 0.000 claims description 2
- 230000008016 vaporization Effects 0.000 claims description 2
- 230000001172 regenerating effect Effects 0.000 claims 1
- 239000011435 rock Substances 0.000 description 30
- 238000000926 separation method Methods 0.000 description 26
- 238000005516 engineering process Methods 0.000 description 18
- 238000010304 firing Methods 0.000 description 9
- 239000013535 sea water Substances 0.000 description 9
- 239000002131 composite material Substances 0.000 description 8
- 238000011084 recovery Methods 0.000 description 8
- 238000004422 calculation algorithm Methods 0.000 description 7
- 230000008901 benefit Effects 0.000 description 6
- 239000000567 combustion gas Substances 0.000 description 6
- 239000005431 greenhouse gas Substances 0.000 description 6
- 238000007599 discharging Methods 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 4
- 230000006835 compression Effects 0.000 description 4
- 238000007906 compression Methods 0.000 description 4
- 238000011161 development Methods 0.000 description 4
- 238000005457 optimization Methods 0.000 description 4
- 238000007616 round robin method Methods 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 150000001875 compounds Chemical class 0.000 description 3
- 238000010276 construction Methods 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 239000003517 fume Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 238000011160 research Methods 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 230000009466 transformation Effects 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 235000011089 carbon dioxide Nutrition 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 230000002950 deficient Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen(.) Chemical compound [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 2
- 238000012827 research and development Methods 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000000740 bleeding effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000012552 review Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
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- 238000002303 thermal reforming Methods 0.000 description 1
- 238000000844 transformation Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 238000012795 verification Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/14—Combined heat and power generation [CHP]
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
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Abstract
一种利用LNG冷分离CO2的燃气轮机发电系统及流程，LNG经过增压泵被压缩，在LNG气化器中加热气化，通过膨胀透平变为常温的天然气，一部分天然气作为燃料进入燃气轮机燃烧室，其余大部分天然气向外界用户输送；被LNG冷却到温度很低的氮气与空气混合，进入压气机；经过压气机增压的气体在回热器中被加热，然后进入燃烧室，与天然气发生燃烧反应后，得到的高温气体再进入透平膨胀作功；透平排气在回热器中被冷却，然后经过热网加热器冷却；在LNG气化器中进一步冷却，多余的氮气在接近环境温度下被排出，凝结的水被回收，并回收到固态CO2。本系统比目前的其它系统效率提高10至15个百分点。
A gas turbine power generation system and process that uses LNG to cool and separate CO 2 . LNG is compressed by a booster pump, heated and gasified in an LNG gasifier, and turned into normal temperature natural gas through an expansion turbine, and part of the natural gas enters the gas turbine as fuel. Combustion chamber, most of the rest of the natural gas is sent to external users; nitrogen cooled to a very low temperature by LNG is mixed with air, and enters the compressor; the gas pressurized by the compressor is heated in the regenerator, and then enters the combustion chamber, and After the combustion reaction of natural gas, the obtained high-temperature gas enters the turbine to expand to do work; the turbine exhaust is cooled in the regenerator, and then cooled by the heat network heater; further cooled in the LNG vaporizer, the excess nitrogen Expelled at near ambient temperature, the condensed water is recovered and recovered as solid CO2 . This system is 10 to 15 percent more efficient than other current systems.
Description
Technical field
The present invention relates to a kind of cold LNG Liquefied natural gas (LNG)
Utilize generation technology and separating carbon dioxide (CO
2) technology carries out the power generation system and the flow process thereof of combination.
Background technique
Technology related to the present invention comprises that mainly LNG is cold at present
Utilize generation technology and CO
2Stripping technique, the state of development and the system features of technology is as follows separately for it.
1, LNG is cold
Utilize generation technology
LNG be a kind of safer, the cleaning the energy.Because rock gas is in liquefaction deep cooling process, the composition of sulphur is separated out, is separated with solid form, so LNG does not contain sulphide.Gas deliquescence process need expend a large amount of compression works, and about 600 times of the rock gas after the liquefaction (LNG) volume-diminished is convenient to remote transportation; Temperature is about-162 ℃, is in the ultralow temperature state, has sizable physical cold
After arriving receiving station, through gasification dispensing user, gasification will discharge a large amount of physical cold again
LNG gasification at present mainly contains three kinds of modes: with seawater or air is that thermal source passes through heat exchanger heating and gasifying (accounting for more than 50%); Submerged combustion vaporizer heating and gasifying (accounting for more than 30%) mainly is used in peak load or annual mean ocean temperature countries and regions on the low side; By heat exchanger cold to LNG
Recycle.Before dual mode do not utilize all that LNG's is cold
And be unfavorable for marine ecology with the seawater LNG that gasifies.
Japan, the U.S. and European Union are cold to LNG
Utilization be put to practicality in a lot of fields.Particularly Japan is owing to lack the energy, and every year, all a large amount of imported L NG were for domestic use.1996 in the energy resource structure of Japan LNG account for 11%, may account for 13% to LNG in 2010.LNG is cold
Successfully utilized in many aspects in the world, as liquefaction separation of air, cold
Generating, cold storage warehouse, liquefaction carbonic acid and dry ice production, low-temperature grinding offal treatment, low temperature medical treatment or the like.China's plan is from external imported L NG, at Shenzhen Eastern construction LNG station, and 3,000,000 tons of imports in 2003 are to 5,000,000 tons of imports in 2010.
Utilize LNG cold
Generating can be divided into two big classes: a class is to utilize LNG cold
Improve the characteristic of power cycle; Another kind of is that low-temperature receiver, environment or low-temperature waste heat are that thermal source is formed relatively independent power generation system with LNG.
Utilize LNG cold
Improve the research and development of power cycle and can trace back to the seventies in 20th century, people such as Greipentrog H. studied the circulation of LNG gasification and closed cycle gas turbine engine combination in 1976.Chiesa P. was cold to utilizing LNG in 1997
Power generation system study, analyze and compared 4 schemes: (1) takes back the Bayton circulatory system of heat.The LNG discharge pressure is 7.0MPa (being used for remote transport gas), set off an explosion for preventing from take place the to reveal danger of (if be medium with air) at the LNG vaporizer, usefulness nitrogen wherein has a spot of oxygen as working medium, content is below 0.5%, to prevent to cause the material nitrogenize.Adopt the Brayton circulation of enclosed, backheat, the LNG gasification makes the compressor inlet gas cooling to-131.6 ℃.Adopt the external combustion mode, turbine inlet temperature is 830 ℃.System effectiveness after the optimization (first law of thermodynamics efficient, the ratio of the external work done of system and the natural gas chemistry calorific value of consumption) is 59.75%,
Efficient (Second Law Efficiency of Thermodynamics, the rock gas of external work done of system and consumption
, LNG cold
The ratio of sum) be 50.61%.(2) compound gas-circulating system.The LNG discharge pressure is 7.0MPa, and the top circulation is conventional gas turbine cycle, and end circulation is the nitrogen circulation of enclosed, and the nitrogen temperature of gas compressor inlet is-147.9 ℃.The top circulation is adopted under the condition of GE LM6000-PC gas turbine, and the system effectiveness after the optimization reaches 63.31%,
Efficient 53.85%.(3) the composite gas circulatory system of band expansion turbine.The LNG discharge pressure is 3.0MPa (being used for the transport gas to combined-cycle power plant), except that the LNG gasification, system is identical with " (2) ", LNG is compressed into 13.0MPa, and (critical pressure of LNG is about 4.6MPa, gasification temperature constantly changes under supercritical pressure, is easy to the cooling procedure coupling with nitrogen; The horizontal evaporator section of isothermal appears in gasification on T-S figure under subcritical pressure boiler, and is bad with the cooling procedure coupling of nitrogen), the gasification back is reduced to 3.0MPa/15 ℃ by the expansion turbine parameter.The nitrogen temperature of gas compressor inlet is-144.7 ℃.The top circulation is adopted under the condition of Siemens V64.3A gas turbine, and the system effectiveness after the optimization reaches 66.19%,
Efficient 55.67%.(4) compound gas-organic working medium circulatory system.The LNG discharge pressure is 3.0MPa.The top circulation is conventional gas turbine cycle, and end circulation is for taking back the enclosed organic working medium (CHF of heat
3) circulation, CHF
3Condensed (85.9 ℃) after the LNG cooling, be pressurized to 14.0MPa by pump.The LNG of 3.0MPa is heated to the saturated gas state in the LNG vaporizer, and the overheated of LNG finished by seawater or river.The top circulation is adopted under the condition of GELM6000-PC gas turbine, and the system effectiveness after the optimization reaches 66.41%,
Efficient 52.15%.The 1st scheme is because adopt the external combustion mode, and the initial temperature of turbine is restricted, and the efficient of system is not high; Three schemes in back still adopt combined cycle, system complex than the efficient height of the 1st scheme.
Utilize LNG cold
Improving the simplest mode of power cycle characteristic is with LNG cooling circulating water one seawater, with the vacuum of raising vapour condenser, thus the efficient of raising Steam Power Circulation or combined cycle.There is not technical problem in this mode, and additional investment is few, and is not having under the condition of LNG power generation system can continue operation.But this mode is cold to LNG
Utilize insufficiently, improve the general less than 1% of efficient of combined cycle.In the system schema that Desideri U. in 2000 etc. propose, utilize a part of LNG cooling to make ocean temperature reduce by 10 ℃, remaining part LNG is after being heated by the exhaust heat boiler smoke evacuation, again by the external work done of expansion turbine.Adopt under the GE6FA gas turbine condition, the most effective of combined cycle system reaches 57.2%,
Efficient reaches 49.1%.They are cold to utilizing LNG in same piece of writing article
Compound gas circulation is studied.The scheme 3 that system schema and Chiesa P. propose is similar, and the top circulation is conventional gas turbine open cycle, and end circulation is the gas circulation of enclosed; The discharge pressure of LNG has two grade: 2.5MPa and 7.3MPa, and a part by the expansion turbine work done, is carried to the user with low pressure behind the heat of another part absorption top circulating exhaust then with the output of high pressure grade after the LNG gasification.To with N
2, He and CO
2Calculate and compare for three kinds of schemes of end cycle fluid, think N
2Circuit systematic function optimum at the bottom of the working medium adopts under the GE7EA gas turbine condition, and system effectiveness is up to 54.2%,
Efficient reaches 47.5%.
Hanawa K. had proposed to utilize LNG cold in 2000
Enclosed Ericsson cycle generating system scheme, high temperature is that 550K, low temperature are 157K, adopt three grades of compressions, three grades of expansions, with the air is working medium, the high temperature heat source of air preheater and secondary reheater is from the mixture of combustion turbine exhaustion in the Combined Cycle Unit and exhaust heat boiler exhaust, and the low temperature cold source of air precooler and secondary inter cooler is from the gasification of LNG.The Ericsson cycle efficiency reaches 35%-37%, is higher than the steam bottom circulating efficiency (about 30%) under the same terms, and is suitable with the Brayton circuit efficient of 1200 ℃ of initial temperature.Temperature after the LNG gasification is-73 ℃, with its low temperature sensible heat the compressor inlet air is cooled off, and can make the Combined Cycle Unit power of corresponding capacity improve 1.1%, and efficient improves 0.4%.Although the heat of the recycling combustion gas of Ericsson and do not consume extra fuel, environment is not polluted, and can satisfy under the summer condition requirement to peak load to the cooling of gas compressor intake air, but this scheme optional equipment (intake air cooler) expense is more, in addition, the Ericsson circulation does not realize the engineering application so far yet.Tsujikawa Y. etc. proposed MGT (Mirror Gas Turbine) in 2000 and utilize LNG cold
Power generation system, as top circulation, be end circulation with conventional gas turbine with the Brayton circulation inverted, that interband is cold, the gasification of a cold employing LNG is cold
Under the condition that adopts 1500 ℃ of grade gas turbines of initial temperature, system effectiveness (different with other system effectiveness definition, as to be the rock gas energy of external work done of system and consumption, the ratio of LNG gasification released cold quantity sum) reaches 55.5%.Utilize LNG cold
Independent generation mode mainly contain: direct expansion method, enclosed Rankine round-robin method, with the two composite algorithm that combines etc.The direct expansion method is heated to superheat state with high pressure LNG with seawater, and by turbine direct expansion work done, the low pressure natural gas after the work done is transported to the user then.The advantage of this mode is that process is simple, and equipment needed thereby is few.But only reclaimed the pressure energy of rock gas, so the amount of work of unit mass LNG is less.Enclosed Rankine round-robin method be with cryogenic LNG as low-temperature receiver, environment (normally seawater) is as thermal source, adopting certain material is that working medium is formed closed cycle.This mode cold
(circulation work done and LNG are cold for the recovery rate
Ratio) higher.Can be divided into single or azeotropic working medium Rankine circulation and non-azeotropic mixed working medium Rankine circulation according to the working medium difference.General LNG adopts Rankine circuit efficient higher when subcritical gasification.Japan Tokyo Gas Co.Ltd. has built a non-azeotropic mixed working medium LNG in countryside, Yokohama cold
The demonstration unit of generating, the vaporization ability of LNG is 5t/h, as thermal source, specified generated output is 130kW with about 24 ℃ seawater.The said firm has developed the working medium of a kind of MFR of being called as, and its main component has methane, ethane, propane etc., so that be complementary with the gasification curve of LNG better, reduces the heat transfer of gasification
Decrease.Composite algorithm combines direct expansion method and enclosed Rankine round-robin method, and cryogenic LNG at first is compressed supercharging, then by condenser heat absorption, drive the enclosed Rankine external work done that circulates, last rock gas is by the gas turbine expansion working, composite algorithm cold
The recovery rate is higher.Cheng Wen dragons in 1999 etc. are cold to several LNG that utilize
The system of generating calculates and compares, under identical design conditions, and direct expansion method, enclosed Rankine round-robin method and composite algorithm cold
The recovery rate is respectively 16.7%, 26.9% and 28.1%.The composite algorithm improvement project that they propose is that the Rankine circulation has been adopted the backheat of bleeding, rock gas to expand and adopted double reheat, makes cold
The recovery rate reaches about 50%.Cheng Wenlong etc. 2000 calculate again to the composite algorithm improvement project, replace seawater as thermal source with the steam discharge of steam turbine, make cold
The recovery rate is brought up to about 55%.And think that this system can avoid the corrosion of seawater heat exchanging equipment.Japan begins to use the LNG generation technology since the seventies in 20th century, utilizes the total capacity of LNG generating to reach about 85MW.Most of generator set adopts composite algorithm, also has to adopt the direct expansion method and take back heat, the generator set of the direct expansion method of heat again, and is cold
The recovery rate is between 13% to 23%.
During with line transportation LNG, need the special material of low temperature, fed distance is long, causes construction cost to increase greatly; And carry the rock gas that has gasified, because of pipe resistance can cause that pressure descends and temperature raises, cause the waste of available energy.If with receiving station and LNG power station separately, effective utilization and Economy two aspects from energy all are irrational.By cold to Japanese LNG
The analysis of generation technology can draw a conclusion: if the LNG of receiving station is useful on generating, then must have a power station will with the integrated construction of LNG receiving station.
Analyze from the world energy sources resource, the overall consumption of whole world rock gas in 1998 reaches 2.340*10
12m
3, increased by 2% than 1997.The LNG amount of importing and exporting by international trade in 1998 is 113 * 10
9m
3, account for 25% of rock gas total volume of trade, increased by 2% than 1997.Therefore research and development efficiently utilizes LNG cold
Generation technology have crucial meaning.
2, CO
2Stripping technique
Since the nineties in 20th century, people recognize that global warming brings serious consequence to human survival and social development, and greenhouse effect are considered to cause the main cause of global warming.Cause the greenhouse gases of greenhouse effect to mainly contain carbon dioxide (CO
2), methane, fluoride, nitrogen oxide etc.Using fossil fuel is to cause CO in the atmosphere
2The basic reason that balance is destroyed.Main one of mode of utilizing of fossil fuel is generating, how to reduce power generation system CO
2Emission level more and more comes into one's own.Raise the efficiency the CO that can correspondingly reduce the unit generating
2Discharge amount, but it is powerless to reducing greenhouse gas emission significantly.Therefore, exploitation is at fuel conversion, combustion process and separation of C O from tail gas
2It is its key technology.
Riemer P. is at IEA greenhouse gases development project (The IEA Greenhouse Gas R ﹠amp; DProgramme) subsidize down, control greenhouse gases technology has been carried out comprehensive review, looked forward to this project and separated, storing CO
2The future action plan.Point out separation of C O
2Make the efficient of generator set reduce about 10 percentage points, cost of electricity-generating improves more than 50%.
The natural gas power system generally adopts combustion gas-Steam Combined Cycle, according to the research of ChiesaP. in 2000, separation of C O
2Technology can reduce 3 classes: separate from gas fume after burning (1), and original power generation system is constant substantially.Can adopt chemiadsorption, physisorphtion and with the absorption method of film separating and combining, same because CO in the flue gas
2Concentration is low, consumes a large amount of mechanical work and heat in separation process, makes system effectiveness reduce about 5 percentage points, and output power descends about 10%.(2) O
2/ CO
2The circulatory system.Circuit working medium in top is CO in combined cycle system
2Increased air separation plant, rock gas and oxygen generation combustion reaction have only CO in the flue gas of generation
2And H
2O, the water separation of being condensed in the cooling procedure of flue gas, the CO that obtains
2Be easy to be recovered.Mathieu P. etc. proposed zero-emission MATIANT circulation in 1999, also belonged to O
2/ CO
2The circuit category.Adopt CO
2The overcritical Rankine circulation of working medium, and backheat and hot again, CO are arranged
2Condensing pressure be that 0.705MPa, adiabatic condensation temperature are 29 ℃, being contracted by pump pressure is pressurized to 30.0MPa, the maximum temperature of high and low pressure regenerator is respectively 600 ℃ and 700 ℃, the turbine initial temperature is 1300 ℃, after the check-off system oxygen wasted work, system effectiveness reaches 44.3%.This system can directly reclaim liquid CO
2(3) system that combines with combined cycle of gas renormalizing.At first rock gas is carried out thermal reforming, obtain CO and H
2, make CO be converted into CO by conversion reaction then
2And H
2, then with CO
2Separate and reclaimed.The hydrogen-rich fuel that obtains generates electricity by the combustion turbine combined circulatory system.
Japanese central power company report in 1989, the said firm utilizes that LNG's is cold
With the isolated CO of power generation system
2Liquefy, reclaim then.The report of Japanese NEDO in 1998 is to separation of C O from mixed gas
2Carried out experimental research, obtained-55 ℃ to 0 ℃ between the vapor liquid equilibrium curve of pressure and concentration.Cold to utilizing LNG
Separation of C O from mixed gas
2Technology study, but with high-temperature gas to isolated solid CO
2Regenerate, and then reclaimed with the measure of conventional compression, this certainly will increase separation of C O
2Wasted work.
Though be the conversion process of fuel or from gas fume after burning separation of C O
2, all to consume extra energy, make the decrease in efficiency of system.With regard to present technical merit, separation of C O
2System effectiveness is descended 5 to 10 percentage points.So separation of C O
2The key of technology is to reduce the energy consumption of separation process.
Summary of the invention
The present invention is primarily aimed at the electricity generating device of the LNG receiving station (being included in the regional LNG receiving stations such as Shenzhen that China's plan is built) that build in all over the world.Utilize LNG cold at present
Power generation system based on generation mode independently, LNG is cold
Utilize and insufficient system's relative complex, and the CO that can not the separating natural gas firing be produced
2
One of purpose of the present invention is to utilize that LNG's is cold
, improve the efficient of power generation system greatly.Adopt gas turbine cycle, the working medium of gas compressor inlet is directly cooled off, make the circuit temperature than being improved with LNG.Adopt internal combustion mode, theoretical air requirement burning, backheat, half-closed gas turbine cycle, thereby for efficiently utilizing LNG cold
Opened up new direction.
Another object of the present invention reclaims CO exactly
2In the LNG gasification, gas fume after burning is cooled off most of CO
2Separate out and be recovered (fraction CO wherein when the external world discharging nitrogen in solid-state mode
2Be discharged from), avoided the shortcoming of a large amount of excess power of consumption that conventional stripping technique brings, thereby be power generation system separation of C O
2New approach is provided.
For achieving the above object, a kind of liquefied natural gas cool that utilizes provided by the invention
The gas turbine generating system of separating carbon dioxide, it comprises half-closed, the backheating gas turbine circulatory system and LNG gasification system, and capital equipment includes:
The LNG vaporizer, with the LNG heating and gasifying and to turbine exhaust cool off;
Gas compressor carries out supercharging to nitrogen and Air mixing gas;
The firing chamber makes rock gas and oxygen generation combustion reaction, obtains high-temperature gas;
Combustion gas turbine makes the high-temperature gas expansion working;
Regenerator heats and the cooling turbine exhaust the gas of blower outlet;
Filter reclaims solid carbon dioxide (CO
2);
Generator.
Remove above-mentioned capital equipment place, this system also includes:
The LNG suction booster compresses the LNG of low pressure;
The rock gas expansion turbine when natural gas transport pressure is subcritical pressure boiler, makes rock gas be expanded to low pressure, normal temperature state, and externally work done;
Heat exchangers for district heating is a supercritical pressure at natural gas transport pressure, utilize the external heat supply water of thermal discharge of turbine exhaust when the cooled temperature of regenerator is still higher.
The pipeline that is connected to common employing between the above each equipment connects.
A kind of liquefied natural gas cool that utilizes provided by the invention
The flow process of the gas turbine generating system of separating carbon dioxide, it is mainly:
LNG is heating and gasifying in the LNG vaporizer, and a part of rock gas acts as a fuel and enters gas-turbine combustion chamber, and all the other most of rock gases are carried to extraneous user;
By LNG be cooled to the very low nitrogen of temperature with from the air mixing of environment, enter gas compressor; Gas through the gas compressor supercharging is heated in regenerator, enters the firing chamber then, and after rock gas generation combustion reaction, the high-temperature gas that obtains enters the turbine expansion work done again; After the turbine exhaust is cooled in regenerator, further cooling in the LNG vaporizer, unnecessary nitrogen is being discharged near under the ambient temperature, and the water that condenses is recovered, and reclaims solid-state CO
2Nitrogen and air mixing are sent to gas compressor.
When being low-pressure, LNG compresses through the LNG suction booster earlier in the flow process of the present invention, then heating and gasifying in vaporizer.
When adopting the supercritical pressure transport gas in the flow process of the present invention, LNG direct gasification, externally heat supply when the cooled temperature of regenerator is still higher; When adopting the subcritical pressure boiler transport gas, LNG is pressurized to supercritical pressure earlier, and heating and gasifying in the LNG vaporizer reclaims its pressure energy by expansion turbine then.
Adopting clean rock gas in the flow process of the present invention is fuel;
Adopt internal combustion, backheating gas turbine single cycle, the working medium of gas compressor inlet is directly cooled off with LNG;
With nitrogen is cycle fluid.
Flow process of the present invention adopts half-closed gas turbine cycle, adds theoretical air requirement at the gas compressor inlet, and in the resultant of combustion reaction, water and carbon dioxide profit are separated, and unnecessary nitrogen is exhausted from system.
The low temperature that produces with the LNG gasification in the flow process of the present invention makes the CO of gaseous state in the turbine exhaust
2Become solid, from mixed gas, separate.Heat exchanger surface heating to stopping transport causes solid-state CO then
2Loosen, come off from heat exchanger surface, reclaim with mechanical means then.
The water vapor that combustion of natural gas produces in the flow process of the present invention is condensed in the LNG vaporizer and is separated out, thus recycle-water.
The nitrogen gas purity of discharging from system in the flow process of the present invention reaches more than 96%, oxygen content is lower than 0.5%.
The present invention is that the generating efficiency of system reaches 70% under 1250 ℃ the condition in the combustion gas turbine initial temperature, nearly 80% the CO that can reclaim that combustion of natural gas generates
2
The present invention is cold thermodynamic cycle, LNG by the system intergration
Integrated utilization and separation of C O
2Organically combine, realized the high efficiency of power generation system and superior environmental-protecting performance; Because system is simple relatively, make power generation system have high property safe and reliable to operation simultaneously; Half-closed backheat cycle generating system is consume water not, concerning the water-deficient area, has improved the engineering possibility of its application greatly; The water that clean combustion of natural gas produces can reclaim, and this also is very attractive power system for the freshwater resources development trend of following growing tension.
With (utilizing LNG) independently generation mode compare, utilize LNG cold
Improve the power system characteristic and more preponderate, it has, and optional equipment lacks and LNG is cold
Utilize advantage more fully.And existing LNG is cold
Utilize power system (mainly comparing), utilize LNG cold with closed cycle with 4 kinds of system schemas of Chiesa P. research
The time, the external combustion mode is adopted in the firing chamber, and system effectiveness is restricted; When adopting conventional internal combustion gas turbine, must adopt end circulation to be the combined cycle system of enclosed again, increased the complexity of system; And the temperature rise of top circulation endothermic process is big, and circuit heat absorption mean temperature is reduced, and is unfavorable to the efficient that improves system.System of the present invention adopts the internal combustion mode, can make full use of the advantage of the high initial temperature of modern gas turbines, and adopts backheat can improve the average endothermic temperature of circuit, for its high efficiency provides assurance; Be fuel, be working medium with nitrogen with the rock gas of cleaning (obtaining after the LNG gasification), can with LNG to turbine exhaust directly cool off, provide condition for adopting half-closed gas turbine single cycle.Therefore cold with existing LNG
Utilize power system to compare, power generation system efficient of the present invention is higher, system is simpler.
Compare with traditional backheating gas turbine circulation, native system has only increased a LNG vaporizer, and it makes the working medium of gas compressor inlet be cooled on the one hand, has improved circuit temperature ratio, makes LNG obtain gasification on the other hand, has the effect that kills two birds with one stone.
Different with traditional closed cycle gas turbine engine circulation, native system adopts half-closed circulation.Add theoretical air requirement (a spot of excess air being arranged) at the gas compressor inlet for keeping gas compressor inlet oxygen stable components, add gas fuel in the firing chamber, in the resultant of combustion reaction, water and carbon dioxide utilize the characteristics of phase transformation separated, unnecessary nitrogen is being exhausted from system near under the normal temperature, has kept the working medium balance of system.The working medium main component that is cooled in the LNG vaporizer is a nitrogen, has guaranteed the safety in operation of LNG vaporizer; For preventing the infringement of pure nitrogen gas, the oxygen of trace is arranged in the working medium that is cooled to material; In near discharging nitrogen under the normal temperature, part of oxygen also is exhausted from system, and can guarantee to remain at 0.5% (this excess oxygen coefficient that has guaranteed the firing chamber simultaneously is more than 1.05) at LNG vaporizer outlet oxygen content by adjusting excess air.
The water vapor that combustion of natural gas produces is condensed in the LNG vaporizer and is separated out, and not only water obtains reclaiming in this process, and by air carry harmful matter---alkaline components can be discharged from, avoided harmful matter to gather intrasystem.
Higher from the unnecessary nitrogen gas purity that system discharges, purity reaches more than 96%, oxygen content is lower than 0.5%, can be used as the technology gas of other industrial process.
The present invention can be according to different natural gas transport pressure ratings and design system.When natural gas transport pressure is supercritical pressure, the LNG direct gasification; When the turbine exhaust when regenerator cooling back temperature is still higher, can cool off it with heat exchangers for district heating earlier, and then send into the LNG vaporizer, the realization cogeneration of heat and power; When natural gas transport pressure was subcritical pressure boiler, LNG was pressurized to supercritical pressure earlier, and gasification is reclaimed its pressure energy by expansion turbine at last then, improved the generating efficiency of system.
With separation of C O
2O
2/ CO
2The circulatory system is compared, and native system does not need to make the air-separating plant of oxygen, has avoided because of making the shortcoming that station service power consumption rate that oxygen brings rises.The present invention utilizes theoretical air requirement combustion manner and nitrogen circulation working medium dexterously, and the main component that makes products of combustion is N
2, CO
2And H
2O is cold for utilizing
Separation of C O
2Created condition.
Present separation of C O
2Technology all be accompanied by lot of energy consumption, the efficient of power generation system is reduced greatly.The low temperature that the present invention utilizes the LNG gasification to produce makes the CO of gaseous state
2Become solid; And to solid-state CO
2The recovery method that adopts heating power and machinery to combine, do not consume extra energy.Therefore there is not energy consumption separation of C O
2Be again of the present invention one big characteristics.
Remove solid-state CO from equipment surface
2Tratitional technology be to heat with the higher gas of temperature, make its distillation for gas.But gaseous state CO
2Must change liquid into the method for compression and cooling could reclaim, and this will consume lot of energy.Combine with heating power and machinery and to reclaim solid-state CO
2It is a new method.The operation of employing switching type is when there is a certain amount of solid-state CO on a row LNG vaporizer surface
2When gathering, switch to the operation of another row LNG vaporizer.The higher relatively nitrogen of temperature of discharging with system heats the heat exchanger surface of stopping transport from the LNG side, and surface temperature raises and causes solid-state CO
2Loosen even come off from heat exchanger surface, use machinery type (as vibration) to reclaim then.In addition, filter is set, collects the solid-state CO that carries in the nitrogen in the downstream of LNG vaporizer
2Adopt this recovery method to consume extra energy hardly.
Reclaim CO
2Reduce the discharging of greenhouse gases, improved the environmental-protecting performance of power generation system; Solid CO
2Can be used as dry ice product and sell, obtain extra economic benefit, thereby improved the Economy of power generation system.
The proposition of this invention based on the grade cascade utilization principle and the system integration method opinion of energy, adopts internal combustion, backheat, high temperature than gas turbine cycle, and efficient height, system are simple; Adopt theoretical air combustion manner and nitrogen circulation working medium, realized directly utilizing LNG low temperature cold
Separation of C O
2Target; Adopt heating power to reclaim solid-state CO with the method that machinery combines
2, do not consume extra energy.
Description of drawings
Below in conjunction with respective drawings specific embodiments of the invention are described in detail.
Fig. 1 is cold for the LNG that utilizes according to the present invention
Separation of C O
2The gas turbine generating system flow chart;
Fig. 2 is cold for the LNG that utilizes according to the present invention
Separation of C O
2The gas turbine generating system structural drawing.
Embodiment
Please referring to Fig. 1 and Fig. 2, major component of the present invention is half-closed, the backheating gas turbine circulatory system and LNG gasification system, in this system: the A-LNG suction booster; The B-gas compressor; The C-firing chamber; The D-combustion gas turbine; The E-regenerator; The F-heat exchangers for district heating; The G-LNG vaporizer; H-rock gas expansion turbine; The I-filter; The J-generator.
Be connected to known technology in the said system, the present invention is not described specifically at this.
System flow is described:
LNG is compressed to state 2 (when LNG has enough pressure this process shouldn't) through suction booster A; LNG is heated and becomes the rock gas 3 of superheat state in LNG vaporizer G; Reach low pressure, normal temperature state 4/5 (expansion turbine being arranged during for subcritical pressure boiler) by expansion turbine H again at natural gas transport pressure; A part of then rock gas 5 acts as a fuel and enters gas-turbine combustion chamber C, and all the other most of rock gases 4 are carried to extraneous user.
Be cooled to the very low nitrogen of temperature (containing minor amounts of oxygen and carbon dioxide) 6 by LNG and mix, reach state 8, enter gas compressor B then with normal temperature, atmospheric air 7 from environment; Gas 9 through the gas compressor supercharging is heated to state 10 in regenerator E; Enter firing chamber C then, after rock gas 5 generation combustion reactions, the high-temperature gas 11 that obtains enters turbine D expansion working again; Turbine exhaust 12 is cooled to state 13 in regenerator E, (natural gas transport pressure is that the temperature of supercritical pressure, state point 13 is when still higher to be reduced to state 14 through heat exchangers for district heating F temperature then, heat exchangers for district heating is arranged) in the system, backwater is heated to state 19 by state 18 in heat exchangers for district heating, feeds to hot user; Mixed gas is further cooled in LNG vaporizer G, and the LNG vaporizer is divided into two sections: the upstream does not have the high temperature section that solid matter (comprising frost and solid carbon dioxide) is separated out for the medium that is cooled, and the downstream is the low-temperature zone that medium has solid matter to separate out that is cooled.Nitrogen (comprising part water vapor and carbon dioxide) 15 is being discharged near under the ambient temperature, and the water 16 that condenses is recovered.The vaporizer of low-temperature zone has two row, adopts the switching type operation, a row operation, and another row reclaim CO
2Be recovered to solid-state CO at the downstream filter I of LNG vaporizer
2(17), the low temperature nitrogen after the filtration reaches state 6, mixes, enters gas compressor with air 7 then.
System flow of the present invention adopts under the different natural gas transport pressure, and certain balance condition performance parameter is referring to table 1-table 4.Relevant condition is: gas compressor polytropic efficiency 86%; Combustion chambers burn efficient 99%; Turbine isentropic efficiency 91%; 1250 ℃ of turbine intake temperature; 20 ℃ of the minimum heat transfer temperature differences of regenerator; 20 ℃/3 ℃ of the minimum heat transfer temperature differences of LNG vaporizer (high-temperature zone of 20 ℃ of corresponding no phase transformations, 3 ℃ to there being the low temperature area of phase transformation); Compressor inlet port crushing 1%; Firing chamber crushing 3%; Regenerator both sides crushing 3%; The side pressure of LNG vaporizer nitrogen decreases 3%; LNG suction booster efficient 76.7%; Rock gas expansion turbine isentropic efficiency 87%; Rock gas expansion turbine inlet valve crushing 0.5MPa; Mechanical efficiency * electric efficiency 96%; The composition of LNG is 100% CH
4
When natural gas transport pressure is 7.0MPa, the gas compressor pressure ratio is 10, the regenerator maximum temperature is that about 700 ℃, LNG consumption are under the condition of 100kg/s, the unit output power reaches 140.02MW, externally heating load is 30.11MW, generating efficiency reaches 62.38%, and power efficieney reaches 75.87%.If regenerator adopts more senior material, get maximum temperature when being 800 ℃, corresponding gas compressor pressure ratio is 6, and generating efficiency reaches 65.62% (externally heat supply).
When natural gas transport pressure was 3.0MPa, the gas compressor pressure ratio was 10, the regenerator maximum temperature is that about 700 ℃, LNG consumption are under the condition of 100kg/s, and the unit output power reaches 148.32MW, and generating efficiency reaches 70.19%,
Efficient reaches 56.35%.
(the gas turbine parameter of choosing in an embodiment comprises turbine initial temperature, compressor efficiency, efficiency of turbine, combustion chambers burn efficient and value of pressure loss everywhere to be 1250 ℃ in the combustion gas turbine initial temperature, through gas turbine performance is carried out verification, substantially meet with the performance of Siemens V64.3A type gas turbine) condition under, yet there are no efficient reach 70% utilize LNG cold
Power generation system.The basic reason that system effectiveness of the present invention is high is: utilize the LNG cooling that the gas compressor inlet temperature is reduced significantly; Adopt the gas turbine cycle of internal combustion, backheat, avoided the low defective of external combustion mode turbine initial temperature, also made full use of the advantage that backheat improves circulation average endothermic temperature.
Utilize LNG to improve the optimal system (the 3rd scheme in the Chiesa P. paper) of thermodynamic cycle performance when adopting Siemens V64.3A type gas turbine at present, generating efficiency is 66.19%, condition in adopting embodiment (and the turbine initial temperature is that 1250 ℃, pressure ratio are 10, natural gas transport pressure be 3.0MPa) is when calculating, generating efficiency is 65.00%, hangs down 5 percentage points than the efficient of native system; Separation of C O in power generation system at present
2Make system effectiveness reduce by 5 to 10 percentage points.Because the advantage of the system intergration and no power consumption separation of C O
2Characteristics, native system improves 10 to 15 percentage points than present system effectiveness.Therefore system of the present invention is utilizing LNG cold
Improve thermal efficiency of cycle and separation of C O
2The aspect has obtained breakthrough.
And system of the present invention and flow process nearly 80% the CO that can reclaim that combustion of natural gas generates
2, and recycle-water and nitrogen, have superior environmental-protecting performance and good technical Economy.
System of the present invention and flow process are simple, operational reliability is high, use conventional gas-turbine plant, and therefore consume water does not have wide future in engineering applications.Table 1 entire system performance data (natural gas transport pressure 7.0MPa)
Table 2 balance condition status parameter (natural gas transport pressure 7.0MPa)
Table 3 entire system performance data (natural gas transport pressure 3.0MPa)
Table 4 balance 212 condition status parameters (natural gas transport pressure 3.0MPa)
*Under 0 ℃ of condition, the water vapor in the mixed gas more than 93% is condensed, and thinks 100% H in the calculating
2O is from this discharge system, and this simplification is very little to the performance impact of system;
*Only consider LNG pressure is risen to from 3.0MPa the pump wasted work of supercritical pressure.Formulae of efficiency in table 1 and the table 3:
| The position | Flow (kg/s) | Pressure (MPa) | Temperature (℃) | The position | Flow (kg/s) | Pressure (MPa) | Temperature (℃) | ||||
| ?1 | ?100.00 | ?0.101 | ?-162.0 | ?11 | ?292.70 | ?0.941 | ?1250.0 | ||||
| ?2 | ?100.00 | ?7.500 | ?-158.0 | ?12 | ?292.70 | ?0.108 | ?698.1 | ||||
| ?3 | ?100.00 | ?7.000 | ?15.0 | ?13 | ?292.70 | ?0.104 | ?146.3 | ||||
| ?4 | ?95.52 | ?7.000 | ?15.0 | ?14 | ?292.70 | ?0.104 | ?50.0 | ||||
| ?5 | ?4.48 | ?7.000 | ?15.0 | ?15 | ?63.38 | ?0.103 | ?0.0 | ||||
| ?6 | ?209.93 | ?0.101 | ?-140.0 | ?16 | ?9.83 | ?0.103 | ?0.0 * | ||||
| ?7 | ?78.28 | ?0.101 | ?15.0 | ?17 | ?9.55 | ?0.101 | ?-140.0 | ||||
| ?8 | ?288.21 | ?0.100 | ?-100.6 | ?18 | ?238.32 | ?0.550 | ?40.0 | ||||
| ?9 | ?288.21 | ?1.000 | ?97.1 | ?19 | ?238.32 | ?0.500 | ?70.0 | ||||
| ?10 | ?288.21 | ?0.970 | ?678.1 | ||||||||
| Gas componant (molar percentage, %) | |||||||||||
| The position | ??6 | ??7 | ??8 | ??11 | ??15 | ||||||
| N 2 | ??99.49 | ??0.79 | ??94.04 | ??91.54 | ??96.12 | ||||||
| O 2 | ??0.50 | ??0.21 | ??5.95 | ??0.46 | ??0.48 | ||||||
| CO 2 | ??0.01 | ??0 | ??0.01 | ??2.67 | ??2.80 | ||||||
| H 2O | ??0 | ??0 | ??0 | ??5.33 | ??0.60 | ||||||
| The position | Flow (kg/s) | Pressure (MPa) | Temperature (℃) | The position | Flow (kg/s) | Pressure (MPa) | Temperature (℃) | ||||
| ?1 | ?100.00 | ?0.101 | ?-162 | ?10 | ?271.34 | ?0.970 | ?678.1 | ||||
| ?2 | ?100.00 | ?13.326 | ?-156.2 | ?11 | ?275.56 | ?0.941 | ?1250.0 | ||||
| ?3 | ?100.00 | ?12.826 | ?118.0 | ?12 | ?275.56 | ?0.108 | ?698.1 | ||||
| ?4 | ?95.78 | ?3.000 | ?15.0 | ?13 | ?275.56 | ?0.104 | ?148.7 | ||||
| ?5 | ?4.22 | ?3.000 | ?15.0 | ?14 | ?275.56 | ?0.104 | ?148.7 | ||||
| ?6 | ?197.64 | ?0.101 | ?-138.4 | ?15 | ?59.67 | ?0.103 | ?0.0 | ||||
| ?7 | ?73.270 | ?0.101 | ?15.0 | ?16 | ?9.26 | ?0.103 | ?0.0 * | ||||
| ?8 | ?271.34 | ?0.100 | ?-99.4 | ?17 | ?8.99 | ?0.101 | ?-138.4 | ||||
| ?9 | ?271.34 | ?1.000 | ?99.6 | ||||||||
| Gas componant (molar percentage, %) | |||||||||||
| The position | ?6 | ?7 | ?8 | ?11 | ?15 | ||||||
| N 2 | ?99.49 | ?0.79 | ?94.04 | ?91.54 | ?96.12 | ||||||
| O 2 | ?0.50 | ?0.21 | ?5.95 | ?0.46 | ?0.48 | ||||||
| CO 2 | ?0.01 | ?0 | ?0.01 | ?2.67 | ?2.80 | ||||||
| H 2O | ?0 | ?0 | ?0 | ?5.33 | ?0.60 | ||||||
Generating efficiency=net power/(gas consumption * rock gas Lower heat value)
Power efficieney=(net power+external heating load)/(gas consumption * rock gas Lower heat value)
Efficient=(net power+externally heat supply
Value)/(cold of gas consumption * rock gas Lower heat value+LNG flow * LNG of unit
)
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