CN103075250B - Method for generating by graded use of cold energy of liquefied natural gas - Google Patents
Method for generating by graded use of cold energy of liquefied natural gas Download PDFInfo
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Abstract
The invention discloses a method for generating by graded use of cold energy of liquefied natural gas, which comprises two parts of natural gas medium Rankine cycle and cold medium Rankine cycle, and is characterized in that vaporized natural gas and another refrigerant are taken as a generating working medium, the pressure of the natural gas medium and the refrigerant medium can be controlled to realize the multiple grades heat exchange with LNG, on one hand, a problem of large available energy loss during a process that the refrigerant recovers the LNG cold energy while Rankine cycle generating can be solved (compared with a conventional method, the method provided by the invention can increase the Rankine cycle efficiency by 60-80% through the usage of LNG cold energy generating), on the other hand, the pressurized cold energy carried by the liquefied refrigerant in the Rankine cycle through system integration can be reused, the utilization efficiency of the cold energy can be enhanced; simultaneously, the heat medium water is taken as a medium, a combustion gas-steam combined power plant near a receiving station is used for generating and the heat medium water is discharged to flue gas waste heat of atmosphere as a low-temperature heat source of cold energy generating, the generating efficiency of Rankine cycle can be enhanced, the waste heat utilization can not generate unfavorable influence on the generating efficiency of the combustion gas power plant, and the thermal pollution of flue gas waste heat on environment can be reduced.
Description
Technical field
The invention belongs to LNG Liquefied natural gas (LNG) cold energy generation field, be specifically related to the method for a kind of cascade utilization cold energy of liquefied natural gas generating.
Background technique
In order to optimize the energy resource structure of China, improve efficiency of energy utilization, reduce CO2 emission, in recent years China's develop actively Gas Industry, the natural gas resource that Devoting Major Efforts To Developing is domestic on the one hand, makes up the deficiency of Domestic Resources on the other hand from external a large amount of inlet natural gas.At present, China in Guangdong, Fujian, Zhejiang, Shanghai, Jiangsu, Shandong, Hebei, the coastal area design and construction such as Liaoning multiple LNG Liquefied natural gas (LNG) station track project.According to General Administration of Customs's publish data display, within 2010, China is total to import 9,360,000 tons of LNG, and the LNG import volume expecting China in 2015 will reach 4,000 ten thousand tons.The LNG of import is the atmospheric low-temperature liquid of a kind of-162 DEG C, needs to utilize pump that LNG is pressurized to 7 ~ 10MPa(absolute pressure, and the pressure hereafter occurred is absolute pressure) after, then be supplied to downstream user to use through the heat vaporized gas ductwork that just can enter.Conventional LNG gasification method adopts seawater or air directly to heat, temperature and ocean temperature lower ground district in the winter time, also need the next heat vaporized LNG of a part of rock gas that burns, so not only a large amount of valuable cold energy is taken away by seawater or air, cause huge energy waste, but also obvious cold pollution can be caused to the water ecological setting of Vaporizing Station periphery.
LNG cold energy is a kind of clean energy resource of very high-quality, and rock gas needs the electric energy of consumption 500 ~ 600kWh/t in the process of liquefaction, can discharge about 230kWh/t cold energy when vaporization.LNG cold energy may be used for the aspects such as air separation, low-temperature cold store, waste old low-temperature grinding to reduce the energy consumption needed for refrigeration, but these amounts needed for cold energy use mode are less, much smaller than the evaporating capacity of an annual millions of tons of LNG receiving station.Utilize cold energy generation facility that LNG cold energy is transformed into electric energy, be a kind ofly large-scale recovery can utilize the mode of receiving station's cold energy, a large amount of low-carbon (LC), green electric energy can be provided for the coastal area of energy scarcity simultaneously.
Developed country pays much attention to the research of LNG cold energy generation technology, the patent application of LNG cold energy generations existing a large amount of at present both at home and abroad, and foreign patent mainly contains:
(1) US Patent No. 2975605 describes a kind of Rankine cycle being refrigerant with ethane or propane by the method for the cryogenic cold energy conversion power generation of LNG.Concrete technology is that cold media air liquefies with LNG heat exchange in heat exchanger, then by pump by after liquid coolant supercharging, utilize seawater or air to be heated vaporization for thermal source, then expanding in turbine produces mechanical energy, thus the generating of driving electric machine.
(2) US Patent No. 3018634 describes a kind of Rankine cycle utilizing ethane and propane two kinds of refrigerant recovering cold energy generations.In the method with ethane and propane successively with LNG heat exchange, reclaim cold energy and liquefy, liquid ethane and propane are by after pump supercharging, be that thermal source is heated vaporization and expansion power generation with air, construct the Rankine cycle of an ethane medium and the Rankine cycle of a propane medium, improve the utilization ratio of LNG cold energy.
(3) US Patent No. 3068659 describes a kind of method of step expansion power generation.In the method with ethane and propane for refrigerant successively with LNG heat exchange, reclaim cold energy and liquefy, liquid ethane and propane, by being expanded step by step by thermal source stepped heating after pump supercharging, are carried out the generating of driving electric machine by the multiple expansion of multiple turbine, improve generating efficiency; And the high-pressure natural gas stepped heating obtained after also being vaporized by LNG also expands step by step, and the pressure energy of high-pressure natural gas is converted to electric energy simultaneously.
(4) US Patent No. 3183666 describes a kind of method that LNG cold energy generation is combined with gas turbine power generation, be the cold energy generation that the Rankine cycle of medium utilizes LNG to vaporize in the method with ethane, Rankine cycle is combined with combustion gas gas turbine power generation process simultaneously, the 440 DEG C of high-temperature flue gas utilizing gas turbine power generation to discharge as thermal source by ethane steam heating to 150 DEG C, improve the generated energy of Rankine cycle.
(5) US Patent No. 4320303 describes a kind of take propane as the method that medium utilizes LNG cold energy generation, in the method with propane for middle refrigerant and LNG heat exchange, propane gas absorbs gas and liquefies, again by utilizing seawater to be heated vaporization after pump supercharging, then high pressure propane steam enters expansion power generation in turbine.
(6) US Patent No. 4330998 describe a kind of with nitrogen and freon for medium utilizes the method for LNG cold energy generation, first utilize nitrogen and LNG heat exchange in that patent and liquefy, liquid nitrogen is by all vaporizing with the Freon gas heat exchange of high temperature after pump supercharging, high pressure nitrogen is expansion work in turbine, and the generating of driving electric machine; Freon absorbs the cold energy of liquid nitrogen and liquefies simultaneously, then after pump supercharging, utilize steam heating to make it vaporize, reflation drive electrical generators group.
(7) that introduces in US Patent No. 4995234 utilizes in LNG cold energy generation method, on the one hand by heat vaporized after LNG supercharging, by the generating of turbine expansion drive electrical generators group, being provided with a set of on the other hand take carbon dioxide as the cold storage of medium and the Rankine cycle of cold energy generation; During peak of power consumption, the cold energy utilizing carbon dioxide absorption LNG to vaporize and liquefying, again by expansion work after pump supercharging and the generating of drive electrical generators group, and during peak of power consumption, then the cold energy carbon dioxide utilizing LNG to vaporize liquefied and be converted into dry ice storage of cold.
(8) US Patent No. 6089028A describes a kind of Rankine cycle utilizing 50% methane to add the mixing coolant media of 50% ethane composition, the high pressure LNG cold energy part discharged of vaporizing evaporates vapour (BOG) cascade EDFA that compresses for LNG in that patent, another part is used for the condensation of 50%-50% methane and ethane mixing cold media air, again by after supercharging after the condensation of mixing refrigerant, the external heat source such as seawater are utilized to be heated vaporization, then expansion work in turbine is entered, and the generating of driving electric machine.
(9) US Patent No. 6367258B1 describes a kind of cold energy and integrated method of integrated gas-steam combined cycle power plant of being vaporized by LNG, the cold energy of LNG is the inlet gas cooling of medium for gas turbine and the exhaust steam pressure of reduction steam turbine by refrigerant, reaches the target improving integrated gas-steam combined cycle power plant efficiency.
In recent years, along with developing rapidly of China LNG industry, LNG cold energy use also receives and pays close attention to widely, and China also applies for (discloses) some cold energy generation patented technologies.
(10) the Chinese invention patent ZL200710027943.3 applied for describes a kind of open type working medium circulation electric power generation method utilizing LNG cold fire, LNG becomes highly pressurised liquid by pump supercharging in the method, all vaporize and become high-pressure natural gas in heat exchanger with after refrigerant heat exchange, then high-pressure natural gas expands and the generating of drive electrical generators group in turbine, natural gas temperature after expansion lower together with LNG in heat exchanger with refrigerant heat exchange, refrigerant provides cold energy to users such as freezers after obtaining the cold energy of LNG and cryogenic natural gas.
(11) Chinese invention patent ZL201010123728.5 describes a kind of integrated optimization method improving generation efficiency of liquefied natural gas cold energy, the mixture of propane or ethane, propane, dichlorodifluoromethane, Freon 13 and monochlorodifluoromethane etc. is utilized all to liquefy for the LNG heat exchange after refrigerant and supercharging in the invention, simultaneously LNG then absorbs heat and all vaporizes, and enters expansion work in turbine and the generating of drive electrical generators group after the low pressure steam of recycling seawater and neighbouring power plant is heated higher temperature; Meanwhile, the refrigerant of liquefaction by after pump supercharging prior to the heat exchange of frozen water backwater, temperature utilizes the low temperature exhaust heats such as the low pressure steam of power plant heat vaporized after raising, and then by turbine expansion acting generating, and Low-temperature Ice coolant-temperature gage can provide air conditioner cold water for administration building, logistics center, maintenance factory building and central control room etc. by Cemented filling after reducing.
Apply for the patent of (disclosing) from above-mentioned these, existingly utilize in the method for LNG cold energy generation, the technology path of generating mainly comprises LNG supercharging vaporization direct expansion generating and the Rankine cycle of coolant media generates electricity two kinds of approach in the middle of utilizing.The generating of direct expansion method utilizes LNG originally as generating working medium, in normal pressure LNG pressurization, in LNG cold energy, some can be converted to pressure energy becomes high-pressure liquid, high-pressure natural gas direct expansion after vaporization can generate electricity by driving electric machine, and Rankine cycle is then that the cryogenic cold energy utilizing high pressure LNG to carry by coolant media generates electricity.Mainly there are the following problems for prior art:
(1) direct expansion method has used high-pressure natural gas direct expansion generating, as US Patent No. 3068659, Chinese patent application 200710027943.3 and Chinese patent ZL201010123728.5, but for LNG receiving station, substantially all require that the rock gas after vaporizing can directly enter high-pressure natural gas pipe network, pressure is at about 7 ~ 10MPa, therefore in most cases, in order to ensure that suction pressure all cannot utilize direct expansion method to utilize the pressure energy of high-pressure natural gas to generate electricity in LNG receiving station.
(2) in the Rankine cycle electricity-generating method utilizing LNG cold energy, select to adopt single hydro carbons or freon to be that coolant media is to reclaim cold energy, as US Patent No. 2975605, US3183666, US4320303, US4995234 etc., because the liquefaction curve of single coolant media differs more with the vaporization curve of LNG, cause exergy loss in cold energy callback course larger, cause generating efficiency lower, when taking seawater as thermal source, generated energy about 20 ~ 25kWh(Wang Kun of LNG cold energy per ton, Analysis of utilization of LNG cold energy for power generation, " cryogenic engineering ", 2005), useful energy utilization ratio is about 21% ~ 25%.
(3) some patent adopts two kinds of refrigerants or mixing refrigerant to reclaim cold energy with LNG heat exchange, as US3018634, US3068659, US4330998, US6089028A etc., although the exergy loss of refrigerant and LNG heat transfer process can be reduced like this, but refrigerant also has a large amount of cold energy not utilize after pump supercharging, directly utilizes low-temperature heat source loss on heating to fall; And the cold energy temperature of LNG comprises the interval from-160 DEG C to 0 DEG C, be difficult to two kinds of refrigerants or a kind ofly mix the cold energy that refrigerant reclaims LNG efficiently, the exergy loss of heat transfer process is still larger, and mixing refrigerant in use some components can lose, thus cause mix refrigerant character change; And because in Rankine cycle, heat source temperature is lower, refrigerant generally cannot utilize the part of temperature more than-40 DEG C in LNG cold energy.
(4) for improving the temperature of thermal source in Rankine cycle, some patents adopt the method integrated with receiving station's periphery plant gas, as US3183666 adopts the high-temperature flue gas of gas turbine, ZL201010123728.5 directly extracts low pressure steam as thermal source, although the efficiency of cold energy generation can be increased like this, the generating efficiency of plant gas but can be reduced.The LNG cold energy of-160 DEG C is directly used for only needing the inlet gas cooling of about 0 DEG C cold energy and reducing steam turbine exhaust pressure by US Patent No. 6367258B1, and cold energy use efficiency is very low.
Summary of the invention
The object of the present invention is to provide the method for a kind of cascade utilization LNG Liquefied natural gas (LNG) cold energy generation, the method utilizes the rock gas and another kind of refrigerant of vaporizing as generating working medium, the multiple step heat exchange with LNG is realized by the pressure controlling gas medium and coolant media, solve the problem that in the process of refrigerant recovering LNG cold energy when Rankine cycle generates electricity, exergy loss is excessive on the one hand, by the system intergration, the cold energy that the liquefaction refrigerant after supercharging in Rankine cycle carries is utilized again on the other hand, improve the utilization ratio of cold energy; Simultaneously, the present invention is discharged to the low-temperature heat source of the fume afterheat of air as cold energy generation with heat medium water after medium utilizes near receiving station gas-steam combined power plants generating electricity, not only can improve the generating efficiency of Rankine cycle, and UTILIZATION OF VESIDUAL HEAT IN can not have a negative impact to the generating efficiency of plant gas, and the thermo-pollution that fume afterheat causes environment can be reduced.
Object of the present invention is achieved through the following technical solutions:
A method for cascade utilization cold energy of liquefied natural gas generating, comprises gas medium Rankine cycle and coolant media Rankine cycle two parts;
Described gas medium Rankine cycle comprises the following steps:
(1) gas medium absorbs cold energy liquefaction
Normal pressure LNG Liquefied natural gas (being called for short LNG) is forced into 7-10MPa, and become high pressure LNG, temperature is about-156 ~-145 DEG C; High pressure LNG and low pressure natural gas heat exchange in low pressure natural gas condenser of discharging from rock gas turbo-expander, low pressure natural gas is liquefied and becomes low pressure LNG, low pressure LNG mixes with the high pressure LNG equipressure flowed out from low pressure natural gas condenser after LNG pump pressurization again; The high pressure LNG obtained after mixing presses heat exchange gas in middle pressure rock gas condenser Yu in extracting out from rock gas turbo-expander, after pressing absorbing natural gas cold energy in this stock, liquefaction becomes middle pressure LNG, pressing LNG to mix with therefrom pressing the high pressure LNG equipressure flowed out in rock gas condenser after pump supercharging again in this, forming high pressure LNG mixing logistics;
(2) gas medium expansion work
The high pressure LNG mixing logistics obtained in step (1) discharges cold energy and all vaporizes and become high-pressure natural gas stream in coolant media Rankine cycle, pressure is about 6-9MPa, in high-pressure natural gas heater, low-temperature heat source is utilized to be heated to 5-10 DEG C again, then separated by the high-pressure natural gas medium being used for circulating generation from high-pressure natural gas stream by shunt, the remaining high-pressure natural gas of being vaporized by LNG enters gas distributing system; In high-pressure natural gas superheater, utilize low-temperature heat source to be done work to entering in rock gas turbo-expander after 40-60 DEG C by the circulation high-pressure natural gas dielectric heating branched away again, and the generating of drive electrical generators group; After expanding, low pressure natural gas pressure medium is reduced to 0.5-1.5MPa, and press rock gas in extracting out from rock gas turbo-expander, its pressure is about 2.0-4.0MPa simultaneously; Gas medium for circulating generation is the 40-70% of LNG evaporating capacity, presses gas medium to account for the 50-70% of generating gas medium total amount in wherein extracting out from rock gas turbo-expander.
Described coolant media Rankine cycle comprises the following steps:
(1) coolant media absorbs cold energy liquefaction
The high pressure LNG mixing logistics obtained in gas medium Rankine cycle is exported the low pressure refrigerant steam heat-exchanging of discharging in low pressure refrigerant condenser Yu from refrigerant turbo-expander, all liquefy after low pressure refrigerant vapor absorption cold energy, highly pressurised liquid refrigerant is become again through refrigerant pump supercharging, then press in entering together with high-pressure natural gas mixing logistics time in refrigerant condenser with extract out from refrigerant turbo-expander time middle press refrigerant steam heat-exchanging, secondary middle pressure refrigerant vapor absorption cold energy post liquefaction is again after refrigerant pump supercharging, new highly pressurised liquid refrigerant stream is mixed into again with the highly pressurised liquid refrigerant equipressure flowed out from low pressure refrigerant condenser, press refrigerant steam heat-exchanging during new highly pressurised liquid refrigerant stream enters middle pressure refrigerant condenser and extracts out from refrigerant turbo-expander together with the high-pressure natural gas mixing logistics flowed out from secondary middle pressure refrigerant condenser and make it liquefy, gas heater is entered after high-pressure natural gas mixing stream temperature is increased to about-10 DEG C, and the middle pressure refrigerant of post liquefaction mixes with pressing the high pressure refrigerant logistics of refrigerant condenser equipressure in outflow after refrigerant pump supercharging, form highly pressurised liquid refrigerant mixing logistics,
(2) coolant media expansion work
The highly pressurised liquid refrigerant mixing logistics obtained in step (1), its pressure is determined according to the type of refrigerant, and requirement can utilize low-temperature heat source to make it all vaporize, and pressure range is about 0.8-2.0MPa; Highly pressurised liquid refrigerant mixing logistics is heated to 40-60 DEG C by the low-temperature heat source utilizing residual heat of electric power plant to provide in refrigerant vaporizer, then enters in refrigerant turbo-expander and does work, and the generating of drive electrical generators group; Circulating refrigerant amount is relevant to refrigerant type, its scope is about the 40-60% of the LNG molar flow that need vaporize, after expanding, the bubble point temperature of low pressure refrigerant is-60 ~-40 DEG C, extract out in one time from refrigerant turbo-expander simultaneously press refrigerant and one in press refrigerant, the bubble point temperature of secondary middle pressure refrigerant is-30 ~-15 DEG C, and the bubble point temperature of middle pressure refrigerant is-10 ~ 0 DEG C; Low pressure refrigerant after expansion and extraction time in pressure and middle pressure refrigerant return in step (1) with high pressure LNG mixing logistics heat exchange.
Low-temperature heat source involved in above-mentioned two kinds of circulations, and the thermal source after the high-pressure natural gas mixture of about-10 DEG C flows to gas heater in coolant media Rankine cycle step (1) is all the heat medium water of employing 60 ~ 80 DEG C, this heat medium water is formed after the waste heat reclaiming the plant gas flue gas be built near LNG receiving station.
In the step (1) of gas medium Rankine cycle, described is divided into low-voltage and medium voltage two strands with the gas medium pressure of LNG heat exchange, and low pressure natural gas pressure medium is about 0.5 ~ 1.5MPa, and the bubble point temperature of its correspondence is about-140 ~-115 DEG C; The pressure of middle pressure gas medium is about 2.0 ~ 4.0MPa, and the bubble point temperature of its correspondence is about-110 ~-85 DEG C.
In coolant media Rankine cycle, described coolant media is ethane, propane, ammonia, carbon dioxide, dichlorodifluoromethane, Freon 13, monochlorodifluoromethane or HFC-134a.
In the step (1) of coolant media Rankine cycle, described is divided into low pressure, secondary middle pressure and middle pressure three strands with the coolant media pressure of high-pressure liquefaction natural gas mixture stream heat exchange, and the bubble point temperature of low pressure refrigerant medium is about-60 DEG C ~-40 DEG C; The bubble point temperature of secondary middle pressure coolant media is about-30 DEG C ~-10 DEG C, and the bubble point temperature of middle pressure coolant media is about-10 DEG C ~ 0 DEG C.
The present invention has following advantage and effect relative to prior art:
(1) method of the present invention is the principle based on cascaded utilization of energy, utilize low pressure natural gas, middle pressure rock gas, low pressure refrigerant, secondary middle pressure refrigerant and middle pressure refrigerant and LNG heat exchange step by step, achieve the utilization step by step of LNG cold energy, reduce the exergy loss of heat transfer LNG and generating working medium diabatic process, cold energy generation efficiency is higher.
(2) the present invention adopts rock gas and refrigerant to build the Rankine cycle utilizing LNG cold energy generation as medium, the rock gas that gas medium obtains after can directly vaporizing with LNG, without the need to purchasing in addition; And the present invention realizes from deep cooling to shallow cold cascade utilization LNG cold energy by the pressure of regulation and control gas medium and coolant media, than using, the coolant media scheme of multiple different boiling is easy to operate, reduces refrigerant acquisition expenses.
(3) liquefaction of subsequent medium will be used further to after medium (gas medium and the coolant media) supercharging of post liquefaction in method of the present invention, as after low pressure liquid natural gas boosting for the liquefaction for secondary middle pressure and middle pressure refrigerant after the liquefaction of middle pressure rock gas, the supercharging of low pressure liquid refrigerant, which enhance the utilization ratio of cold energy in Rankine cycle.
(4) method of the present invention utilizes heat medium water to reclaim plant gas near LNG receiving station discharged to the low-temperature heat source of the fume afterheat in air as Rankine cycle, not only can improve the generating efficiency in Rankine cycle, and the generating efficiency of plant gas can not be reduced, and the thermo-pollution of power-plant flue gas to atmosphere environment can be reduced.
(5) method of the present invention recycles LNG cold energy by multistage step, recovered flue gas heat improves the heat source temperature of Rankine cycle, adopt method of the present invention, the generated energy of LNG cold energy per ton can reach 40 ~ 45kWh, utilizes the Rankine cycle efficiency of LNG cold energy generation to improve 60 ~ 80% than routine.
Accompanying drawing explanation
Fig. 1 is the workflow diagram of the method for cascade utilization cold energy of liquefied natural gas of the present invention generating; Wherein: 1,3,6-LNG Liquefied natural gas (LNG) pump A, B, C; 2-low pressure natural gas condenser; 4,7-LNG mixer A, B; Rock gas condenser is pressed in 5-; 8-low pressure refrigerant condenser; 9,11,14-liquid coolant pump A, B, C; Pressure refrigerant condenser in 10-time; 12,15-liquid coolant mixer A, B; Refrigerant condenser is pressed in 13-; 16-refrigerant vaporizer; 17-refrigerant turbo-expander; 18,23-generator set A, B; 19-high-pressure natural gas heater; 20-high-pressure natural gas shunt; 21-high-pressure natural gas superheater; 22-rock gas turbo-expander; 24-flue gas heat-exchange unit; 25,29-heat medium water conveyance conduit; 26-heat medium water shunt; 27-heat medium water mixer; 28-heating agent water pump;
Logistics is illustrated as follows:
lNG/ natural gas stream;
coolant media logistics;
plant gas flue gas stream;
heat medium water logistics.
Embodiment
Below in conjunction with embodiment and accompanying drawing, the present invention is described in further detail, but embodiments of the present invention are not limited thereto, and for the process parameter do not indicated especially, can refer to routine techniques and carry out.
Embodiment
A method for cascade utilization cold energy of liquefied natural gas generating, its technological process as shown in Figure 1, comprises gas medium Rankine cycle and coolant media Rankine cycle two parts;
The LNG Liquefied natural gas (LNG) mole of receiving station consists of: methane 96.64%, ethane 2.77%, propane 0.34%, isobutane 0.07%, butane 0.08%, nitrogen 0.10%; The LNG that cold energy generation utilizes is 100.0t/h, and the coolant media that cold energy generation is selected is propane.
Gas medium Rankine cycle comprises the following steps:
(1) gas medium absorbs cold energy liquefaction
The normal pressure that need vaporize, the LNG Liquefied natural gas (LNG) of-162 DEG C are pressurized to 10.0MPa by LNG pump 1, and become high pressure LNG, temperature rises to-156.0 DEG C.High pressure LNG and the 20.0t/h, the 0.61MPa that discharge from rock gas turbo-expander 22 end, low pressure natural gas heat exchange low pressure natural gas condenser 2 of-73.6 DEG C, low pressure natural gas all liquefies becomes low pressure LNG, and temperature is reduced to-134.6 DEG C, this low pressure LNG is pressurized to 10.0MPa through LNG pump 3 again, is then about-121.6 DEG C with the high pressure LNG(temperature flowed out from low pressure natural gas condenser 2) in LNG mixer 4, equipressure mixes, the high pressure LNG(flow obtained after mixing is 120.0t/h, temperature is-122.0 DEG C) in middle pressure rock gas condenser 5 with the 46.0t/h that extracts out from rock gas turbo-expander 22,-12.3 DEG C, heat exchange gas is pressed in 2.70MPa, after pressing rock gas to obtain cold energy in this strand, all liquefaction becomes the middle pressure LNG of-98.4 DEG C, LNG is pressed to recycle LNG pump 6 by its boost in pressure to 10.0MPa in this, temperature is increased to-87.4 DEG C, then in LNG mixer 7 ,-73.9 DEG C are about with therefrom pressing the high pressure LNG(temperature flowed out in rock gas condenser 5) isobaric to mix, form high pressure LNG mixing logistics, due to the pressure loss of heat transfer process, this strand of high pressure LNG mixture flowing pressure is about 9.6MPa, temperature is about-77.4 DEG C, and flow is 166.0t/h.
(2) gas medium expansion work
High pressure LNG mixing logistics (166.0t/h) that step (1) obtains discharges cold energy and all vaporizes and becomes high-pressure natural gas stream in coolant media Rankine cycle, because heat transfer process exists the pressure loss, the Pressure Drop of high-pressure natural gas stream is to 9.0MPa, in high-pressure natural gas heater 19, utilize the heat medium water of 52.0 DEG C to be heated to about 10 DEG C again, then the high-pressure natural gas medium 66.0t/h being used for circulating generation is separated from this high-pressure natural gas stream by high-pressure natural gas shunt 20, all the other high-pressure natural gas of being vaporized by LNG (100.0t/h) enter gas distributing system, the high-pressure natural gas medium separated utilizes the heat medium water of 70 DEG C that it is heated to 55 DEG C further in high-pressure natural gas superheater 21, then enter expansion work in rock gas turbo-expander 22, and drive electrical generators group 23 generates electricity, the end outlet pressure of rock gas turbo-expander 22 is 0.63MPa, and by pressing gas medium 46.0t/h in punching extraction 2.72MPa in the middle of rock gas turbo-expander 22, the isentropic efficiency of rock gas turbo-expander 22 is 0.7, and mechanical efficiency is 0.96, and output power is 2365kW.
Coolant media Rankine cycle comprises the following steps:
(1) coolant media absorbs cold energy liquefaction
The 166.0t/h obtained in the step (1) of gas medium Rankine cycle ,-77.4 DEG C, the high pressure LNG mixing logistics of 9.6MPa discharge in low pressure refrigerant condenser 8 and from refrigerant turbo-expander 17 end outlet 51.6t/h ,-33.4 DEG C, 0.07MPa low-pressure propane steam heat-exchanging, after absorbing heat, high pressure LNG mixing logistics is all vaporized, temperature is increased to-52.3 DEG C, then enters time middle pressure refrigerant condenser 10; And also all liquefy after low-pressure propane vapor absorption cold energy, temperature is reduced to-51.3 DEG C, and the low-pressure propane of post liquefaction is pressurized to 1.6MPa by recycling liquid coolant pump 9, temperature is about-50.3 DEG C, then enters in time middle pressure refrigerant condenser 10.In secondary middle pressure refrigerant condenser 10, the 58.0t/h extracted out from refrigerant turbo-expander 17 stage casing,-7.5 DEG C, pressure propane vapor and 166.0t/h in 0.2MPa time, the high-pressure natural gas of-52.3 DEG C and 51.6t/h, the highly pressurised liquid propane heat exchange of-50.3 DEG C, secondary middle pressure propane vapor absorbs cold energy and all liquefies, temperature is about-25.5 DEG C, recycle liquid coolant pump 11 by its boost in pressure to 1.6MPa, then carry out equipressure with the highly pressurised liquid propane (temperature about-26.7 DEG C) flowed out from secondary middle pressure refrigerant condenser 10 in liquid refrigerant within mixer 12 and be mixed into new highly pressurised liquid refrigerant stream, its flow is 109.6t/h, temperature is-25.5 DEG C, and also rising to-26.7 DEG C from the high-pressure natural gas temperature that secondary middle pressure refrigerant condenser 10 flows out, this high-pressure natural gas enters middle pressure refrigerant condenser 13 together with the new highly pressurised liquid refrigerant stream flowed out from liquid coolant mixer 12.In middle pressure refrigerant condenser 13, the 39.0t/h extracted out from refrigerant turbo-expander 17,10 DEG C, press in 0.4MPa propane vapor absorb the cold energy of high-pressure natural gas and highly pressurised liquid propane and all liquefy, temperature is reduced to-6.4 DEG C, then 1.6MPa is pressurized to by liquid coolant pump 14, in refrigerant mixer 15 Yu therefrom, the high pressure propane liquid flowed out in refrigerant condenser 13 is pressed to be mixed into highly pressurised liquid propane mixed flow again, mixed temperature is-7.8 DEG C, and flow is 148.6t/h.
(2) coolant media expansion work
1.6MPa, 148.6t/h highly pressurised liquid propane mixed flow obtained in step (1) enters in refrigerant vaporizer 16, the 70 DEG C of heat medium waters produced by power-plant flue gas waste heat are utilized to be heated whole vaporization, temperature is increased to 55 DEG C, then enter expansion work in refrigerant turbo-expander 17, and drive electrical generators group 18 generates electricity; The outlet pressure of refrigerant turbo-expander 17 is 0.077MPa, and presses propane gas 39.0t/h by extracting out in 0.20MPa time in the punching of refrigerant turbo-expander 17 stage casing in pressure propane gas 58.0t/h and 0.40MPa.The isentropic efficiency of refrigerant turbo-expander 17 is 0.7, and mechanical efficiency is 0.96, and output power is 2855kW.
Low-temperature heat source in gas medium Rankine cycle and coolant media Rankine cycle is the 70 DEG C of heat medium waters reclaiming power-plant flue gas waste heat and produce.In 1110.0t/h, the heat medium water of the 49.0 DEG C plant gas near receiving station, the flue gas of 90 ~ 100 DEG C that utilize power plant to discharge by flue gas heat-exchange unit 24 is heated 70 DEG C, is then transported to cold energy generation device district by heat medium water conveyance conduit 25.In heat medium water shunt 26, heat medium water is divided into two strands: one is about 1050.0t/h, and to enter refrigerant vaporizer 16 all heat vaporized by highly pressurised liquid propane, temperature is increased to 55 DEG C, and the heat load of refrigerant vaporizer 16 is 18963kW, and heat medium water temperature is reduced to 54.4 DEG C from 70 DEG C; Another strand of heat medium water is about 60.0t/h and enters high-pressure natural gas superheater 21, and by 66.0t/h high-pressure natural gas dielectric heating to 55 DEG C, heat exchange load is about 2393kW, and after heat exchange, heating agent coolant-temperature gage is reduced to 38.3 DEG C from 70 DEG C; The two strands of heat medium waters flowed out from refrigerant vaporizer 16 and high-pressure natural gas superheater 21 mix in heat medium water mixer 27, temperature is 52.0 DEG C, then enter high-pressure natural gas heater 19 and 166.0t/h ,-8.6 DEG C of high-pressure natural gas are heated to 10 DEG C, heat exchange load 3419kW.The hot water temperature of flowing out from high-pressure natural gas heater 19 is reduced to 49.6 DEG C, then sends plant gas and flue gas heat exchange by after heat medium water supercharging by heat medium water conveyance conduit 29 by heating agent water pump 28, forms heat recovery circulation.
In whole cold energy generation device, LNG pump, the isentropic efficiency of liquid coolant pump and heating agent water pump gets 0.75, and mechanical efficiency gets 0.96, and in running, the power consumption of LNG pump 1,3,6 is respectively 876kW, 184kW and 408kW; The power consumption of liquid coolant pump 9,11,14 is respectively 51kW, 56kW, 36kW; Heating agent water pump 28 lift 30mH
2o, power consumption is 130kW.The isentropic efficiency of rock gas turbo-expander 22 and refrigerant turbo-expander 17 gets 0.70, and mechanical efficiency gets 0.96, and output work is respectively 2365kW and 2855kW.Consider that when not carrying out cold energy use, the LNG of normal pressure also needs supercharging to vaporize, and therefore the power consumption of LNG pump 1 is not counted in the consumption of cold energy generation.Whole cold energy generation system utilizes the clean output work 4355kW of the LNG cold energy of 100t/h, and the generated energy of average LNG cold energy per ton is 43.6kWh, improves 74.4% than conventional LNG cold energy Rankine cycle generated energy 25kWh/t.The low temperature useful energy of 10MPa ,-156 DEG C of LNG is about 101.6kWh/t, and utilize LNG cold energy generation exergy efficiency of the present invention to be 42.9%, comparatively conventional method useful energy utilization ratio 21 ~ 25% is greatly improved.
Above-described embodiment is the present invention's preferably mode of execution; but embodiments of the present invention are not restricted to the described embodiments; change, the modification done under other any does not deviate from Spirit Essence of the present invention and principle, substitute, combine, simplify; all should be the substitute mode of equivalence, be included within protection scope of the present invention.
Claims (5)
1. a method for cascade utilization cold energy of liquefied natural gas generating, is characterized in that comprising gas medium Rankine cycle and coolant media Rankine cycle two parts;
Described gas medium Rankine cycle comprises the following steps:
(1) gas medium absorbs cold energy liquefaction
Normal pressure LNG Liquefied natural gas is forced into 7-10MPa, becomes high pressure LNG, temperature is-156 ~-145 DEG C; High pressure LNG and low pressure natural gas heat exchange in low pressure natural gas condenser of discharging from rock gas turbo-expander, low pressure natural gas is liquefied and becomes low pressure LNG, low pressure LNG mixes with the high pressure LNG equipressure flowed out from low pressure natural gas condenser after LNG pump pressurization again; The high pressure LNG obtained after mixing presses heat exchange gas in middle pressure rock gas condenser Yu in extracting out from rock gas turbo-expander, after pressing absorbing natural gas cold energy in this stock, liquefaction becomes middle pressure LNG, pressing LNG to mix with therefrom pressing the high pressure LNG equipressure flowed out in rock gas condenser after pump supercharging again in this, forming high pressure LNG mixing logistics;
(2) gas medium expansion work
The high pressure LNG mixing logistics obtained in step (1) discharges cold energy and all vaporizes and become high-pressure natural gas stream in coolant media Rankine cycle, pressure is 6-9MPa, in high-pressure natural gas heater, low-temperature heat source is utilized to be heated to 5-10 DEG C again, then separated by the high-pressure natural gas medium being used for circulating generation from high-pressure natural gas stream by shunt, the remaining high-pressure natural gas of being vaporized by LNG enters gas distributing system; In high-pressure natural gas superheater, utilize low-temperature heat source to be done work to entering in rock gas turbo-expander after 40-60 DEG C by the circulation high-pressure natural gas dielectric heating branched away again, and the generating of drive electrical generators group; After expanding, low pressure natural gas pressure medium is reduced to 0.5-1.5MPa, and press rock gas in extracting out from rock gas turbo-expander, its pressure is 2.0-4.0MPa simultaneously; Gas medium for circulating generation is the 50-70% of LNG evaporating capacity, presses gas medium to account for the 50-70% of generating gas medium total amount in wherein extracting out from rock gas turbo-expander;
Described coolant media Rankine cycle comprises the following steps:
(1) coolant media absorbs cold energy liquefaction
The high pressure LNG mixing logistics obtained in gas medium Rankine cycle is exported the low pressure refrigerant steam heat-exchanging of discharging in low pressure refrigerant condenser Yu from refrigerant turbo-expander, all liquefy after low pressure refrigerant vapor absorption cold energy, highly pressurised liquid refrigerant is become again through refrigerant pump supercharging, then press in entering together with high-pressure natural gas mixing logistics time in refrigerant condenser with extract out from refrigerant turbo-expander time middle press refrigerant steam heat-exchanging, secondary middle pressure refrigerant vapor absorption cold energy post liquefaction is again after refrigerant pump supercharging, new highly pressurised liquid refrigerant stream is mixed into again with the highly pressurised liquid refrigerant equipressure flowed out from low pressure refrigerant condenser, press refrigerant steam heat-exchanging during new highly pressurised liquid refrigerant stream enters middle pressure refrigerant condenser and extracts out from refrigerant turbo-expander together with the high-pressure natural gas mixing logistics flowed out from secondary middle pressure refrigerant condenser and make it liquefy, gas heater is entered after high-pressure natural gas mixing stream temperature is increased to-10 DEG C, and the middle pressure refrigerant of post liquefaction mixes with pressing the high pressure refrigerant logistics of refrigerant condenser equipressure in outflow after refrigerant pump supercharging, form highly pressurised liquid refrigerant mixing logistics,
(2) coolant media expansion work
Refrigerant vaporizer utilizes low-temperature heat source that the highly pressurised liquid refrigerant mixing logistics obtained in step (1) is heated to 40-60 DEG C, then enters in refrigerant turbo-expander and does work, and the generating of drive electrical generators group; Circulating refrigerant amount is the 40-60% of the LNG molar flow that need vaporize, after expanding, the bubble point temperature of low pressure refrigerant is-60 ~-40 DEG C, extract out in one time from refrigerant turbo-expander simultaneously press refrigerant and one in press refrigerant, the bubble point temperature of secondary middle pressure refrigerant is-30 ~-15 DEG C, and the bubble point temperature of middle pressure refrigerant is-10 ~ 0 DEG C; Low pressure refrigerant after expansion and extraction time in pressure and middle pressure refrigerant return in step (1) with high pressure LNG mixing logistics heat exchange.
2. the method for cascade utilization cold energy of liquefied natural gas generating according to claim 1, it is characterized in that: low-temperature heat source involved in two kinds of circulations, and the thermal source after the high-pressure natural gas mixture of-10 DEG C flows to gas heater in coolant media Rankine cycle step (1) is all the heat medium water of employing 60 ~ 80 DEG C, this heat medium water is formed after the waste heat reclaiming the plant gas flue gas be built near LNG receiving station.
3. the method for cascade utilization cold energy of liquefied natural gas generating according to claim 1, it is characterized in that: in the step (1) of gas medium Rankine cycle, described is divided into low-voltage and medium voltage two strands with the gas medium pressure of LNG heat exchange, low pressure natural gas pressure medium is 0.5 ~ 1.5MPa, and the bubble point temperature of its correspondence is-140 ~-115 DEG C; The pressure of middle pressure gas medium is 2.0 ~ 4.0MPa, and the bubble point temperature of its correspondence is-110 ~-85 DEG C.
4. the method for cascade utilization cold energy of liquefied natural gas generating according to claim 1, it is characterized in that: in coolant media Rankine cycle, described coolant media is ethane, propane, ammonia, carbon dioxide, dichlorodifluoromethane, Freon 13, monochlorodifluoromethane or HFC-134a.
5. the method for cascade utilization cold energy of liquefied natural gas generating according to claim 1, it is characterized in that: in the step (1) of coolant media Rankine cycle, described is divided into low pressure, secondary middle pressure and middle pressure three strands with the coolant media pressure of high-pressure liquefaction natural gas mixture stream heat exchange, and the bubble point temperature of low pressure refrigerant medium is-60 DEG C ~-40 DEG C; The bubble point temperature of secondary middle pressure coolant media is-30 DEG C ~-10 DEG C, and the bubble point temperature of middle pressure coolant media is-10 DEG C ~ 0 DEG C.
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| CN112963731B (en) * | 2021-03-10 | 2022-04-26 | 江苏科技大学 | Integrated intermediate medium vaporizer with cold energy utilization and power generation system formed by same |
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| EP4191177A1 (en) | 2021-12-01 | 2023-06-07 | Nederlandse Organisatie Voor Toegepast- Natuurwetenschappelijk Onderzoek Tno | Lng exergy optimization for sbcc |
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