CN100424450C - Method for using cooling capacity of LNG with cooling media as medium and apparatus thereof - Google Patents
Method for using cooling capacity of LNG with cooling media as medium and apparatus thereof Download PDFInfo
- Publication number
- CN100424450C CN100424450C CNB2006101236638A CN200610123663A CN100424450C CN 100424450 C CN100424450 C CN 100424450C CN B2006101236638 A CNB2006101236638 A CN B2006101236638A CN 200610123663 A CN200610123663 A CN 200610123663A CN 100424450 C CN100424450 C CN 100424450C
- Authority
- CN
- China
- Prior art keywords
- refrigerant
- natural gas
- liquefied natural
- cold
- heat exchanger
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Images
Landscapes
- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
The utilization of liquefied natural gas with coolant as medium mainly refers to the coolant as the medium to exchange heat with liquefied natural gas in the receiving station, and sending cooled coolant through coolant heat insulation pipe to the cooled energy utilization zone outside the receiving station for customer's use. The equipment applying this method comprises a liquefied natural gas pump, a sea water carburetor, a low temperature heat exchanger, a coolant low temperature reserving tank, a low temperature coolant pump, a coolant normal temperature reserving tank and normal temperature coolant pump. It is simple in operation, convenient to control, feasible to set multi big scale cooled energy utilization to make the best of it.
Description
Technical field
The present invention relates to the technical field of liquefied natural gas (LNG) cryogenic energy utilization, particularly a kind of is that the cold energy of liquefied natural gas of medium utilizes method and device thereof with the refrigerant.
Background technology
The lay equal stress on planning of accelerated development natural gas industry of exploitation of formulating according to country and introduction, China will be before 2010 build several large-scale LNG receiving stations, the LNG of the up to ten million tons of annual import in the southeastern coastal areas.Liquefied natural gas (LNG) is a natural gas through depickling, processed ,-162 ℃ the cryogenic liquid that forms by the low temperature process cryogenic liquefaction.The LNG that produces 1 ton approximately needs power consumption 850kWh, and can emit a large amount of colds when vaporizing in receiving station, is about 830～860kJ/kg.This a part of cold will cause severe energy waste as not being used, and the environment of LNG receiving station periphery is caused cold pollution.Utilize the cold of LNG, the purpose of can reach energy savings, increasing economic efficiency by specific technology.
At present, doing number of research projects aspect the LNG cryogenic energy utilization both at home and abroad, existing LNG cryogenic energy utilization mode is directly to utilize devices such as the same air separation of LNG, cryogenic pulverization, freezer to carry out heat exchange mostly, and main patented technology comprises:
(1) " cold on gasifying liquefied natural gas utilize method " of Chinese invention patent " 00128935.7 ", it adopts recirculated water to reach the purpose of air-conditioning temperature-reducing as refrigerant.Because water to 0 ℃ will be frozen into ice, water is with-162 ℃ LNG heat exchange, and cold fire is very big with loss in the diabatic process, and very easily causes moisture freezes Cheng Bing, blocking pipe.
(2) Chinese invention patent " 01127133.7 ", " 200510022599.X " (application number), utility model patent " 2005202000306.8 ", and the cold of having introduced several LNG of utilization in the United States Patent (USP) " US5137558 " carries out the device of air separation, these air-separating plants all are directly to utilize outer defeated high pressure LNG with the circulating nitrogen gas heat exchange, utilize the cold of LNG to cool off the circulating nitrogen gas of low temperature compression and normal temperature compressed air, the energy consumption of air-separating plant is significantly reduced.
(3) introduced the refrigerating plant that a kind of LNG of utilization cold is used for freezer in the Chinese utility model patent " 200420114636.0 ", wherein directly utilize LNG to make it liquefaction with the cold-producing medium heat exchange of freezer, and then liquid refrigerant is transported to freezer evaporation, provide cold to freezer.This method has been simplified the cooling flow of freezer greatly, can save the initial outlay of freezer, reduces operating cost greatly.
(4) Chinese utility model patent " 02264657.4 " has been introduced a kind of device that utilizes cold energy of liquefied natural gas semiconductor temperature differential generating and hydrogen manufacturing, it is characterized in that semiconductor thermoelectric generator is close to respectively on low-temperature receiver heat exchanger that LNG flows through and the thermal source heat exchanger that has seawater to flow through by the cold and hot end face of thermoelectric pile sheet makes, and semiconductor thermoelectric generator sends direct current in the time of seawater heating LNG; This power supply is connected to the both positive and negative polarity of electrolytic cell, and brine electrolysis generates hydrogen and oxygen; The part seawater is sent to the heat exchanger that seawater is a thermal source after removing to cool off the alkali lye of brine electrolysis earlier again.Cooling water when wherein seawater is hydrogen manufacturing is again the heating source of LNG, has improved the semiconductor generating efficiency; To reclaim LNG cold electricity and be used for hydrogen manufacturing, save the cooling water that heat exchanger area and hydrogen manufacturing consume, also save the required alternating current-direct current change device of generating and hydrogen manufacturing, the water electrolysis hydrogen production cost is greatly reduced.
Above-mentioned patented technology all is directly to utilize LNG with directly carrying out heat exchange with device for cooling, because LNG receiving station generally all is located near the harbour, usually land resource is limited, and the use in soil costs an arm and a leg, and is difficult to large-scale cryogenic energy utilization project layout within receiving station; And the LNG cold of receiving station is huge, and the refrigeration requirement of unitem is less relatively, and receiving station can't hold a plurality of cryogenic energy utilization projects, thereby causes the cold of LNG fully not recycle.If LNG is transported to cold user outside the receiving station by hot insulated line, then since the LNG vaporescence not under receiving station directly controls, so can't be according to the gas downstream user carry out safe way with the gas demand fluctuation.Owing to limited by the place, and all LNG can not be transported to outside the receiving station again and vaporize, so existing LNG cryogenic energy utilization project is all more single, and scale is limited, and the cryogenic energy utilization rate of LNG is not high.
Summary of the invention
In order to overcome above-mentioned the deficiencies in the prior art part, it is liquefied natural gas (LNG) the cryogenic energy utilization method of medium with the refrigerant that primary and foremost purpose of the present invention is to provide a kind of.The present invention is simple to operate, and control is convenient, and a plurality of large-scale cryogenic energy utilization projects can be set, and makes the cold of liquefied natural gas be fully used.
Another object of the present invention is to provide that a kind of what realize said method is the cold energy of liquefied natural gas use device of medium with the refrigerant.
Purpose of the present invention is achieved through the following technical solutions: a kind of is that the cold energy of liquefied natural gas of medium utilizes method with the refrigerant, comprises the steps and process conditions:
(1) cold recovery
The LNG pump is extracted-162 ℃ liquefied natural gas out from storage tank, liquefied natural gas pressure is increased to 7.0～10.0MPa, and temperature is elevated to-158.0～-151.6 ℃; Above-mentioned high-pressure liquefaction natural gas is divided into two strands, and wherein one enters cryogenic heat exchanger and vaporizes with the refrigerant heat exchange; Another strand enters the seawater vaporizer and vaporizes with seawater to make heat exchange; High-pressure natural gas after the vaporization enters the natural gas high pressure pipe network; When total evaporating capacity of liquefied natural gas changed, the amount that control enters the high-pressure liquefaction natural gas of seawater vaporizer and cryogenic heat exchanger satisfied the vaporization demand; When refrigerant heat-exchange system (comprising cryogenic heat exchanger, refrigerant feed-line and storage tank thereof etc.) when breaking down, make whole high-pressure liquefaction natural gases all through the vaporization of seawater vaporizer, guarantee air feed safety.
(2) cryogenic energy utilization
The refrigerant that will be in cryogenic heat exchanger obtains cold with the liquefied natural gas heat exchange is transported to the cryogenic energy utilization district outside the receiving station, refrigerant is reduced to normal pressure through the choke valve throttling, and it is stored in the refrigerant low-temperature storage tank, because this moment, refrigerant was in the height supercooled state, so refrigerant still can remain liquid phase after the throttling step-down; According to the cold size of cold user needs, the low temperature refrigerant pump carries refrigerant to give the cold user then; Refrigerant utilizes cold through the user, after temperature raises with its conveying and be stored in the refrigerant normal temperature storage tank; By the normal temperature refrigerant pump refrigerant is carried back cryogenic heat exchanger again, form cold recovery, utilize circulation.
In order to realize the present invention better, in the step (1), when total evaporating capacity of described liquefied natural gas changes, at first enter the amount of the high-pressure liquefaction natural gas of seawater vaporizer vaporization, and the liquefied natural gas amount that maintenance enters in the cryogenic heat exchanger is constant by adjusting; In the time only can't meeting the demands by the evaporating capacity of regulating the seawater vaporizer, then regulate the amount that enters the high-pressure liquefaction natural gas of heat exchange vaporization in the cryogenic heat exchanger, corresponding adjusting simultaneously is with the coolant quantity of high-pressure liquefaction heat exchange gas, to satisfy needed liquefied natural gas vaporization amount.
In the step (1), the amount that described control enters the high-pressure liquefaction natural gas of seawater vaporizer and cryogenic heat exchanger is to control by the liquefied natural gas flow pilot angle valve and the liquefied natural gas flow valve of band shunting.
In the step (2), described low temperature refrigerant pump carries refrigerant to give the cold user, is to control the conveying capacity of the refrigerant that is supplied to the cold user by regulating low temperature cold medium flux valve.
In the step (2), described normal temperature refrigerant pump is carried back cryogenic heat exchanger with refrigerant, is the normal temperature coolant quantity of carrying back cryogenic heat exchanger by the valve regulation of normal temperature cold medium flux.
Be filled with refrigerant in the described cryogenic heat exchanger.The major function of refrigerant is exactly to reclaim cold wherein with the liquefied natural gas heat exchange and flow to the cold user who is positioned at outside the receiving station as medium to use.The cold that refrigerant carries can be used for air separation, deep cooling is pulverized, made dry ice, freezer refrigerating, can also be used for the air inlet cooling of cold generating and gas turbine.Owing to not limited by the land used of receiving station,, make the cold of liquefied natural gas be fully used so a plurality of large-scale cryogenic energy utilization projects can be set.
In order to prevent that refrigerant solidifies in the process of liquefied natural gas heat exchange, generally require the freezing point of refrigerant to be lower than-160 ℃.Described refrigerant can be hydrocarbon or CFC.Described hydrocarbon can be ethane, propane, ethene or propylene etc.Described fluorochlorohydrocarbon is a dichlorodifluoromethane.
What realize said method is the cold energy of liquefied natural gas use device of medium with the refrigerant, comprises liquefied natural gas pump, seawater vaporizer, cryogenic heat exchanger, refrigerant low-temperature storage tank, low temperature refrigerant pump, refrigerant normal temperature storage tank and normal temperature refrigerant pump etc.; Described liquefied natural gas pump is connected with cryogenic heat exchanger with the seawater vaporizer respectively by liquefied natural gas flow pilot angle valve, the liquefied natural gas flow valve of band shunting successively, and seawater vaporizer, cryogenic heat exchanger are connected with the natural gas high pressure pipe network by the natural gas flow metered valve respectively; Cryogenic heat exchanger is connected with the refrigerant low-temperature storage tank with choke valve by refrigerant insulation feed-line successively, and the refrigerant low-temperature storage tank is connected with the low temperature refrigerant pump, and the low temperature refrigerant pump is connected with refrigerant normal temperature storage tank by low temperature cold medium flux valve; Refrigerant normal temperature storage tank is connected with the normal temperature refrigerant pump, and the normal temperature refrigerant pump is connected with cryogenic heat exchanger with normal temperature refrigerant feed-line by normal temperature cold medium flux valve successively, forms cold recovery, utilizes circulation.
Since the gas downstream user with gas load in time, seasonal fluctuation is bigger, nonuniformity coefficient with gas is bigger, thereby receiving station must have certain air feed peak modulation capacity, promptly when usefulness gas peak, downstream, pass through to increase the evaporating capacity of liquefied natural gas, that satisfies downstream user uses the gas demand, then reduces the evaporating capacity of liquefied natural gas with the gas low ebb time.When the evaporating capacity of LNG fluctuates widely, the evaporating capacity that liquefied natural gas flow pilot angle valve and the liquefied natural gas flow valve by accommodation zone shunting changes the seawater vaporizer.When adjustable range surpasses the regulating power of seawater vaporizer, then regulate by the LNG evaporating capacity that changes cryogenic heat exchanger.The evaporating capacity of liquefied natural gas and refrigerant heat exchange changes in time, thereby causes being supplied to cold user's cold instability.On the other hand, the cold user also may can not keep absolute constant because of factors such as turn of the market, weather conditions variation fluctuate to some extent to the demand of cold.For this reason, two refrigerant storage tanks in the flow process of the present invention will play the effect that solves vaporization and the nonsynchronous problem of cryogenic energy utilization duration of load application characteristic.The low temperature refrigerant pump is extracted the coolant quantity of delivering to the cold user out from the refrigerant low-temperature storage tank, be (by the low temperature cold medium flux valve) controlled according to cold user's demand.Refrigerant temperature after utilizing cold is increased near normal temperature, and its flow that turns back to refrigerant normal temperature storage tank remains unchanged.And the normal temperature refrigerant is carried back the flow of cryogenic heat exchanger by refrigerant normal temperature feed-line by the normal temperature refrigerant pump, be (by the normal temperature cold medium flux valve) controlled according to the demand of the evaporating capacity of liquefied natural gas.Because above-mentioned duration of load application characteristic difference, the feed flow of synchronization refrigerant pump is different.By the lifting of refrigerant low-temperature storage tank and refrigerant normal temperature tank level, just can guarantee to satisfy simultaneously nonsynchronous vaporization and cryogenic energy utilization workload demand within the specific limits.Concrete operations are: in the time need increasing the liquefied natural gas vaporization amount with the gas peak, improve the conveying capacity of normal temperature refrigerant by the aperture that increases normal temperature cold medium flux valve; Because the flow of low temperature cold medium flux valve does not change, so the liquid level in the refrigerant low-temperature storage tank raises and the corresponding reduction of liquid level of refrigerant normal temperature storage tank gradually; With the gas low ebb time, need reduce the evaporating capacity of liquefied natural gas, then reduce the conveying capacity of normal temperature refrigerant by the aperture that reduces the cold medium flux valve, same because the not change of the flow of low temperature cold medium flux valve, so the liquid level of refrigerant raises in the refrigerant normal temperature storage tank, the liquid level in the refrigerant low-temperature storage tank reduces; By utilizing the adjusting of these two refrigerant storage tanks, can be implemented in recovery cold as much as possible under the situation of liquefied natural gas vaporization amount fluctuation, that satisfies the different times downstream simultaneously uses the gas demand.
The present invention has following advantage and beneficial effect with respect to prior art:
(1) by utilizing refrigerant as medium, cold recovery and cryogenic energy utilization are separately become two processes, only the very little cryogenic heat exchanger of floor space is placed in the liquefied natural gas receiving station, and the cold user that floor space is big is arranged in outside the liquefied natural gas receiving station, only supplies cold by receiving station to each cold user by the refrigerant feed-line.The vaporescence of liquefied natural gas is all under the direct control of liquefied natural gas receiving station, like this can be according to the gas downstream user come the evaporating capacity of condition lng with gas load variations rule, what ensure the downstream uses the gas demand, is not subjected to the influence of cryogenic energy utilization fully.
(2) adjusting by refrigerant low-temperature storage tank and refrigerant normal temperature storage tank, can satisfy under the situation of liquefied natural gas vaporization amount fluctuation, the cold of recovery liquefied natural gas as much as possible, improved the recovery utilization rate of cold, and can provide cold to the user more stably, certain regulating power is also arranged when cold user's load fluctuation.
(3) existing cold energy of liquefied natural gas utilize in the technology all be adopt the high-pressure liquefaction natural gas directly and the cryogenic energy utilization device carry out heat exchange, the cold user must use high voltage bearing heat exchanger (more than the 7.0MPa) to utilize the cold of liquefied natural gas, and possess corresponding emergency service, make the investment of cryogenic energy utilization project increase like this.And the present invention utilizes refrigerant as medium, and the low temperature refrigerant is transported to the cold user, and refrigerant pressure is far below the pressure for vaporization of liquefied natural gas, and the investment of heat exchanger can greatly reduce in the cryogenic energy utilization project, improves the economic benefit of cryogenic energy utilization project.
(4) cold that carries of refrigerant can be used for that air separation, deep cooling are pulverized, system dry ice, freezer refrigerating, the air inlet that can also be used for cold generating and gas turbine is cooled off.Owing to not limited by the land used of receiving station,, can also make the cold of liquefied natural gas to be fully used according to the principle of " temperature counterpart, cascade utilization " so a plurality of large-scale cryogenic energy utilization projects can be set.
Description of drawings
Fig. 1 utilizes the structure principle chart of method for cold energy of liquefied natural gas of the present invention.
The specific embodiment
The present invention is described in further detail below in conjunction with embodiment and accompanying drawing, but embodiments of the present invention are not limited thereto.
As shown in Figure 1, the present invention is the cold energy of liquefied natural gas use device of medium with the refrigerant, comprise liquefied natural gas pump 1, the liquefied natural gas flow pilot angle valve 2 of band shunting, liquefied natural gas flow valve 3, seawater vaporizer 5, cryogenic heat exchanger 6, natural gas flow metered valve 7, natural gas flow metered valve 8, low temperature refrigerant feed-line, choke valve 11, refrigerant low-temperature storage tank 12, low temperature refrigerant pump 13, low temperature cold medium flux valve 14, refrigerant normal temperature storage tank 16, normal temperature refrigerant pump 17, normal temperature cold medium flux valve 18 and normal temperature refrigerant feed-line 19.Liquefied natural gas pump 1 is connected with seawater vaporizer 5 with liquefied natural gas flow valve 3 by the liquefied natural gas flow pilot angle valve 2 of band shunting successively, liquefied natural gas pump 1 is connected with cryogenic heat exchanger 6 with liquefied natural gas flow valve 4 by the liquefied natural gas flow pilot angle valve 2 of band shunting successively, and seawater vaporizer 5 is connected with natural gas high pressure pipe network 9 by natural gas flow metered valve 7; Cryogenic heat exchanger 6 is connected with natural gas high pressure pipe network 9 by natural gas flow metered valve 8; Cryogenic heat exchanger 6 is connected with refrigerant low-temperature storage tank 12 with choke valve 11 by refrigerant insulation feed-line 10 successively, and refrigerant low-temperature storage tank 12 is connected with low temperature refrigerant pump 13, and low temperature refrigerant pump 13 is connected with refrigerant normal temperature storage tank 16 by low temperature cold medium flux valve 14; Refrigerant normal temperature storage tank 16 is connected with normal temperature refrigerant pump 17, and normal temperature refrigerant pump 17 is connected with cryogenic heat exchanger 6 with normal temperature refrigerant feed-line 19 by normal temperature cold medium flux valve 18 successively, forms cold recovery, utilizes circulation.
A certain Large LNG receiving station, year Liquefied Natural Gas Import (LNG) 3,000,000 tons, wherein 1,000,000 tons/year are used for retail, and remaining 2,000,000 tons/year liquefied natural gas vaporization enters pipe network and flows to downstream user and use, and mean annual evaporating capacity is about 228 tons/hour.The mole of liquefied natural gas consists of: methane 96.62%, ethane 2.77%, propane 0.34%, iso-butane 0.07%, butane 0.08%, nitrogen 0.10%.Cold user 12 mainly contains large cold storage and junked tire low-temperature grinding factory that produces 30000 tons of fine glue powders per year of three 10,000 tons, and total cold load is about 18.9MW.
Liquefied natural gas pump 1 is per hour extracted-162 ℃, 228 tons liquefied natural gas out from storage tank, and its pressure is increased to outer defeated required pressure scope, about 8.0MPa (high pressure LNG), and the LNG temperature is increased to about-158.0 ℃ approximately.In the liquefied natural gas flow pilot angle valve 2 of band shunting, the liquefied natural gas of high pressure is divided into two strands, by condition lng flow valve 3 and liquefied natural gas flow valve 4, one LNG of 128 tons/hour is entered seawater vaporizer 5 through liquefied natural gas flow valve 3 vaporize with seawater to make heat exchange, the LNG that another strand is 100 tons/hour enters cryogenic heat exchanger 6 through liquefied natural gas flow valve 4 and vaporizes with the refrigerant heat exchange.Refrigerant is selected propane, and flow is 210 tons/hour, and temperature is 15 ℃, and pressure is 1.0MPa.By with the liquefied natural gas heat exchange, propane obtains cold, and temperature is reduced to-150 ℃ approximately, and pressure is 0.95MPa, and liquefied natural gas obtains heat and all vaporizes simultaneously, and is heated to about 5.0 ℃.After 6 vaporizations of high-pressure liquefaction natural gas via seawater vaporizer 5 and cryogenic heat exchanger, enter natural gas high pressure pipe network 9 through natural gas flow metered valve 7 and natural gas flow metered valve 8 respectively and flow to the gas downstream user and use.
About-150 ℃ propane is transported to cryogenic energy utilization district liquefied natural gas receiving station outside by refrigerant hot insulated line 10, because course of conveying has loss of refrigeration capacity, temperature rises to-148.0 ℃ approximately, and while pressure is reduced to 0.90MPa.Propane is depressurized to 0.10MPa by choke valve 11 again, and the low temperature propane of this normal pressure is stored in the refrigerant low-temperature storage tank 12.Utilize low temperature refrigerant pump 13 that normal pressure propane is boosted to 1.20MPa, temperature rises to-147.1 ℃, is transported to cold user 15 through low temperature cold medium flux valve 14 then and supplies with user's use.The cold that propane carries is after cold user 15 uses, temperature is increased to about 12.0 ℃, it is carried back and is stored in the refrigerant normal temperature storage tank 16, and through normal temperature cold medium flux valve 18 and normal temperature refrigerant feed-line 19 delivery of propane of normal temperature is returned cryogenic heat exchanger 6 by normal temperature refrigerant pump 17, form a cold recovery and utilize circulation.
The evaporating capacity of liquefied natural gas is subjected to the influence of gas downstream user gas consumption, therefore also has tangible inhomogeneities, the evaporating capacity of liquefied natural gas generally average magnitude ± 20% scope in the fluctuation, promptly the evaporating capacity of liquefied natural gas fluctuates between 182.4～273.6 tons/hour.Under 100 tons of/hour constant situations of evaporating capacity that keep cryogenic heat exchanger 6, satisfy the liquefied natural gas vaporization demand of different time sections by the evaporating capacity of regulating seawater vaporizer 5, promptly the evaporating capacity of seawater vaporizer 5 fluctuates between 82.4～173.6 tons/hour.The liquefied natural gas flow pilot angle valve of in operating process, shunting 2 by accommodation zone, liquefied natural gas flow valve 3 and liquefied natural gas flow valve 4 are controlled the treating capacity of seawater vaporizer 5 and cryogenic heat exchanger 6, promptly the time with the gas low ebb, the evaporating capacity of liquefied natural gas is 182.4 tons/hour, wherein 100 tons/hour liquefied natural gas advances cryogenic heat exchanger 6 vaporizations and reclaims cold, and 82.4 tons of/hour remaining liquefied natural gas advance in the seawater vaporizer to vaporize; With the gas peak time, the evaporating capacity of liquefied natural gas reaches 273.6 tons/hour, the liquefied natural gas flow pilot angle valve 2 of accommodation zone shunting then, liquefied natural gas flow valve 3 and liquefied natural gas flow valve 4, keep 100 tons/hour of the treating capacities of cryogenic heat exchanger 6 constant, and the evaporating capacity of seawater vaporizer 5 is increased to 173.6 tons/hour from 82.4 tons/hour.In this way, can effectively tackle the fluctuation of liquefied natural gas vaporization amount, guarantee air feed safety to the gas downstream user.
In embodiment 1 described liquefied natural gas (LNG) receiving station, developing along with cryogenic energy utilization market, cold user 15 increases by one and produces 200000 tons of liquia air product (90,000 tons/year of liquid oxygen per year on the basis of original large cold storage and junked tire low-temperature grinding factory, 12.5 ten thousand tons/year of liquid nitrogen, 0.4 ten thousand tons/year of liquid argons) air separation plant, its refrigeration duty is about 16.5MW, and cold user 15 total load reaches 35.4MW.In order to satisfy the refrigeration requirement that cold user 15 increases, liquefied natural gas flow pilot angle valve 2 by the accommodation zone shunting, liquefied natural gas flow valve 3 and liquefied natural gas flow valve 4,170 tons/hour liquefied natural gas are passed through cryogenic heat exchanger 6 with the propane heat exchange, increase is to the cold of cold user 15 supplies, and the evaporating capacity of seawater vaporizer 5 is reduced to 58 tons/hour liquefied natural gas simultaneously.Because liquefied natural gas (LNG) amount by cryogenic heat exchanger 6 vaporization increases, also increase to 355 tons/hour by 210 tons/hour with the propane amount of liquefied natural gas heat exchange.By heat exchange, the propane temperature is reduced to-151.6 ℃, and is transported to cryogenic energy utilization district outside the liquefied natural gas receiving station by refrigerant hot insulated line 10, because course of conveying has loss of refrigeration capacity, the propane temperature rises to about-148.0 ℃, and pressure is reduced to 0.90MPa.Propane is depressurized to 0.10MPa by choke valve 11 again, and this atmospheric low-temperature propane is stored in the refrigerant low-temperature storage tank 12.Utilize low temperature refrigerant pump 13 that normal pressure propane is boosted to 1.20MPa, temperature rises to-147.1 ℃, is transported to cold user 15 through low temperature cold medium flux valve 14 then and supplies with user's use.The cold that propane carries is after cold user 15 uses, temperature is increased to about 12 ℃, it is stored in the refrigerant normal temperature storage tank 16, and through normal temperature cold medium flux valve 18 and normal temperature refrigerant feed-line 19 delivery of propane of normal temperature is returned cryogenic heat exchanger 6 by normal temperature refrigerant pump 17, form a cold recovery and utilize circulation.
Because the inhomogeneities of gas downstream user usefulness gas load, thus the also fluctuation in time of the evaporating capacity of liquefied natural gas, generally average magnitude ± fluctuate in 20% scope, promptly the evaporating capacity of liquefied natural gas fluctuates between 182.4～273.6 tons/hour.Keep 58 tons/hour of the evaporating capacities of seawater vaporizer 5 constant, then the vaporization of cryogenic heat exchanger 6 load is 124.4～215.6 tons/hour a liquefied natural gas.Therefore the propane amount with the liquefied natural gas heat exchange also fluctuates in time in cryogenic heat exchanger 6, fluctuation range is 260～450 tons/hour, this mainly regulates by regulating normal temperature cold medium flux valve 18 change delivery of propane amounts, when the evaporating capacity that is cryogenic heat exchanger 6 is 124.4 tons/hour a liquefied natural gas, carrying back the propane amount of low-temperature heat exchange 6 through normal temperature refrigerant pump 17 is 260 tons/hour, when the vaporization load of cryogenic heat exchanger 6 reaches 215.6 tons of/hour liquefied natural gas, regulate normal temperature refrigerant pump 18, make through normal temperature refrigerant pump 17 and carry back the propane amount of low-temperature heat exchange 6 also to be increased to 450 tons/hour accordingly.If it is stable that cold user 15 refrigeration requirement keeps, then regulate low temperature refrigerant valve 14 and make low temperature refrigerant pump 13 that 350 tons/hour, about-150 ℃ propane per hour is provided to cold user 15.In this way, can effectively tackle the fluctuation of liquefied natural gas vaporization amount, guarantee air feed safety to the gas downstream user.
Claims (8)
1. one kind is that the cold energy of liquefied natural gas of medium utilizes method with the refrigerant, it is characterized in that comprising the steps and process conditions:
(1) cold recovery
The LNG pump is extracted-162 ℃ liquefied natural gas out from storage tank, liquefied natural gas pressure is increased to 7.0～10.0MPa, and temperature is elevated to-158.0～-151.6 ℃; Above-mentioned high-pressure liquefaction natural gas is divided into two strands, and wherein one enters cryogenic heat exchanger and vaporizes with the refrigerant heat exchange; Another strand enters the seawater vaporizer and vaporizes with seawater to make heat exchange; High-pressure natural gas after the vaporization enters the natural gas high pressure pipe network: when total evaporating capacity of liquefied natural gas changed, the amount that control enters the high-pressure liquefaction natural gas of seawater vaporizer and cryogenic heat exchanger satisfied the vaporization demand;
(2) cryogenic energy utilization
The refrigerant that will be in cryogenic heat exchanger obtains cold with the liquefied natural gas heat exchange is transported to the cryogenic energy utilization district outside the receiving station, refrigerant is reduced to normal pressure through the choke valve throttling, and it is stored in the refrigerant low-temperature storage tank, the cold size that needs according to the cold user carries refrigerant to give the cold user by the low temperature refrigerant pump then; Refrigerant utilizes cold through the cold user, after temperature raises with its conveying and be stored in the refrigerant normal temperature storage tank; By the normal temperature refrigerant pump refrigerant is carried back cryogenic heat exchanger again, form cold recovery, utilize circulation.
2. according to claim 1 a kind of be that the cold energy of liquefied natural gas of medium utilizes method with the refrigerant, it is characterized in that: in the described step (1), when total evaporating capacity of described liquefied natural gas changes, at first enter the amount of the high-pressure liquefaction natural gas of seawater vaporizer vaporization, and the liquefied natural gas amount that maintenance enters in the cryogenic heat exchanger is constant by adjusting; In the time only can't meeting the demands by the evaporating capacity of regulating the seawater vaporizer, then regulate the amount that enters the high-pressure liquefaction natural gas of heat exchange vaporization in the cryogenic heat exchanger, corresponding adjusting simultaneously is with the coolant quantity of high-pressure liquefaction heat exchange gas.
3. according to claim 1 a kind of be that the cold energy of liquefied natural gas of medium utilizes method with the refrigerant, it is characterized in that: in the described step (1), described control enters the amount of the high-pressure liquefaction natural gas of seawater vaporizer and cryogenic heat exchanger, is to control by the liquefied natural gas flow pilot angle valve and the liquefied natural gas flow valve of band shunting.
4. according to claim 1 a kind of be that the cold energy of liquefied natural gas of medium utilizes method with the refrigerant, it is characterized in that: in the step (2), described low temperature refrigerant pump carries refrigerant to give the cold user, is to control the conveying capacity of the refrigerant that is supplied to the cold user by regulating low temperature cold medium flux valve.
5. according to claim 1 a kind of be that the cold energy of liquefied natural gas of medium utilizes method with the refrigerant, it is characterized in that: in the step (2), described normal temperature refrigerant pump is carried back cryogenic heat exchanger with refrigerant, is the normal temperature coolant quantity of carrying back cryogenic heat exchanger by the valve regulation of normal temperature cold medium flux.
6. according to claim 1 a kind of be that the cold energy of liquefied natural gas of medium utilizes method with the refrigerant, it is characterized in that: described refrigerant is hydrocarbon or CFC.
7. according to claim 6 a kind of be that the cold energy of liquefied natural gas of medium utilizes method with the refrigerant, it is characterized in that: described hydrocarbon is ethane, propane, ethene or propylene; Described fluorochlorohydrocarbon is a dichlorodifluoromethane.
8. one kind is the cold energy of liquefied natural gas use device of medium with the refrigerant, comprises liquefied natural gas pump, seawater vaporizer, cryogenic heat exchanger, refrigerant low-temperature storage tank, low temperature refrigerant pump, refrigerant normal temperature storage tank and normal temperature refrigerant pump; It is characterized in that: described liquefied natural gas pump is connected with cryogenic heat exchanger with the seawater vaporizer respectively by liquefied natural gas flow pilot angle valve, the liquefied natural gas flow valve of band shunting successively, and seawater vaporizer, cryogenic heat exchanger are connected with the natural gas high pressure pipe network by the natural gas flow metered valve respectively; Cryogenic heat exchanger is connected with the refrigerant low-temperature storage tank with choke valve by refrigerant insulation feed-line successively, and the refrigerant low-temperature storage tank is connected with the low temperature refrigerant pump, and the low temperature refrigerant pump is connected with refrigerant normal temperature storage tank by low temperature cold medium flux valve; Refrigerant normal temperature storage tank is connected with the normal temperature refrigerant pump, and the normal temperature refrigerant pump is connected with cryogenic heat exchanger with normal temperature refrigerant feed-line by normal temperature cold medium flux valve successively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006101236638A CN100424450C (en) | 2006-11-21 | 2006-11-21 | Method for using cooling capacity of LNG with cooling media as medium and apparatus thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006101236638A CN100424450C (en) | 2006-11-21 | 2006-11-21 | Method for using cooling capacity of LNG with cooling media as medium and apparatus thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1963347A CN1963347A (en) | 2007-05-16 |
| CN100424450C true CN100424450C (en) | 2008-10-08 |
Family
ID=38082494
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2006101236638A Expired - Fee Related CN100424450C (en) | 2006-11-21 | 2006-11-21 | Method for using cooling capacity of LNG with cooling media as medium and apparatus thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100424450C (en) |
Families Citing this family (30)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009126604A1 (en) * | 2008-04-11 | 2009-10-15 | Fluor Technologies Corporation | Methods and configuration of boil-off gas handling in lng regasification terminals |
| CN101852529B (en) * | 2010-05-28 | 2012-10-31 | 华南理工大学 | Method and device for efficient utilization of pressure energy of natural gas pipeline network |
| CN102563777A (en) * | 2010-12-31 | 2012-07-11 | 中国石油天然气集团公司 | System for collecting cold energy of liquefied natural gas in drilling team |
| CN102331127A (en) * | 2011-08-23 | 2012-01-25 | 华南理工大学 | Method and device for making ice by using liquefied natural gas cold energy |
| CN102431640A (en) * | 2011-11-22 | 2012-05-02 | 杨彦华 | LNG (liquefied natural gas) powered refrigeration ship |
| CN103151967B (en) * | 2013-01-27 | 2015-06-10 | 南京瑞柯徕姆环保科技有限公司 | Cold energy thermoelectric power generating device |
| CN103234318B (en) * | 2013-04-12 | 2015-09-23 | 广州华丰能源科技有限公司 | A kind of apparatus and method utilizing cold energy of liquefied natural gas demist ice making |
| CN104215105B (en) * | 2014-08-28 | 2016-06-22 | 华南理工大学 | The LNG heat-exchange method of a kind of anti-freeze and device |
| CN104296284B (en) * | 2014-10-14 | 2017-08-22 | 谢红飞 | A kind of method for the utilization ratio for improving cold on gasifying liquefied natural gas |
| CN104595707B (en) * | 2014-12-30 | 2016-06-29 | 西安交通大学 | A kind of gain recycling system of cold energy of liquefied natural gas |
| CN104654007B (en) * | 2015-03-16 | 2017-02-22 | 西北工业大学 | Ethylene supply device and flow measuring method thereof |
| CN104964157A (en) * | 2015-07-09 | 2015-10-07 | 江苏中圣高科技产业有限公司 | Method and device for improving liquefied natural gas gasification energy-saving efficiency |
| CN105258258B (en) * | 2015-09-17 | 2017-03-22 | 张守庆 | Data center air conditioning system based on liquefied natural gas (LNG) cold energy application and application method thereof |
| CN105241262B (en) * | 2015-11-03 | 2017-10-20 | 中冶东方工程技术有限公司 | A kind of heating furnace pure oxygen burning and carbon dioxide capture systems and technique |
| CN107304974B (en) * | 2016-04-25 | 2023-07-07 | 江苏德邦工程有限公司 | Liquefied natural gas cold energy recovery system and method |
| EP3483401A4 (en) * | 2016-07-06 | 2020-06-03 | Cytroniq Co., Ltd. | System using cold energy |
| CN106288082A (en) * | 2016-08-23 | 2017-01-04 | 庹华明 | A kind of industry liquid nitrogen cold recovery system |
| CN106545935B (en) * | 2016-10-27 | 2019-07-05 | 航天科工哈尔滨风华有限公司 | It is a kind of using intermediate medium gasifier as the air-conditioning system of cold source |
| CN106679263A (en) * | 2016-12-07 | 2017-05-17 | 深圳市欣华兴节能科技有限公司 | Liquid nitrogen cooling capacity recycling device and control method |
| CN106764414A (en) * | 2016-12-27 | 2017-05-31 | 常州大学 | A kind of LNG gasification station cold, heat and power triple supply system |
| CN106642800B (en) * | 2017-01-24 | 2022-09-20 | 江苏德邦工程有限公司 | LNG (liquefied Natural gas) gasification cold energy refrigeration house system and cold energy recovery method thereof |
| CN107449199A (en) * | 2017-07-27 | 2017-12-08 | 苏州吉云新材料技术有限公司 | A kind of energy-saving cryogenic energy utilization system |
| KR102117852B1 (en) * | 2018-07-02 | 2020-06-03 | 주식회사래티스테크놀로지 | Fluid Tank Having Internal Vaporizers |
| CN109556984B (en) * | 2018-12-07 | 2021-08-31 | 合肥通用机械研究院有限公司 | Rapid inflation precooling system and use method thereof |
| CN109708000B (en) * | 2019-02-25 | 2020-08-18 | 北方工业大学 | L-CH2 type hydrogen station heat management system |
| CN111219596B (en) * | 2020-03-03 | 2024-05-24 | 佛燃能源集团股份有限公司 | Electric cooling production recycling system of hydrogenation station and natural gas pressure regulating station |
| CN111912059A (en) * | 2020-07-13 | 2020-11-10 | 西安工程大学 | Evaporative cooling air-conditioning system combining roof spraying cooling and floor radiation |
| CN115479421A (en) * | 2021-06-15 | 2022-12-16 | 中集安瑞科能源装备（苏州）有限公司 | Operating system for storing, recovering and supplying cold energy |
| CN113701049B (en) * | 2021-09-09 | 2023-04-25 | 液空厚普氢能源装备有限公司 | Intelligent recovery control system and control method for cold energy of liquid hydrogen hydrogenation station |
| CN114216046B (en) * | 2022-01-20 | 2024-10-18 | 浙江浙能技术研究院有限公司 | LNG cold energy and data center cold supply coupling system and method |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3724229A (en) * | 1971-02-25 | 1973-04-03 | Pacific Lighting Service Co | Combination liquefied natural gas expansion and desalination apparatus and method |
| US4329842A (en) * | 1980-07-02 | 1982-05-18 | Hans D. Linhardt | Power conversion system utilizing reversible energy of liquefied natural gas |
| JPH0926228A (en) * | 1995-07-07 | 1997-01-28 | Eibisu:Kk | Method for utilizing heat energy and cold energy contained in liquefied natural gas, and system for utilizing heat energy and cold energy contained in liquefied natural gas |
| CN1295646A (en) * | 1998-03-27 | 2001-05-16 | 埃克森美孚上游研究公司 | Producing power from pressurized liquefied natural gas |
| CN1342879A (en) * | 2000-09-13 | 2002-04-03 | 谢红飞 | Method for utilizing cold on gasifying liquefied natural gas |
| CN1447016A (en) * | 2002-03-22 | 2003-10-08 | 中国科学院工程热物理研究所 | Gas turbine generating system and flow by cooling liquefied natural gas to separate carbon dioxide |
| CN2602186Y (en) * | 2002-09-24 | 2004-02-04 | 中国科学技术大学 | Semiconductive temperature difference power generating and hydrogen production apparatus using cold energy of liquefied natural gas |
| JP2004211949A (en) * | 2002-12-27 | 2004-07-29 | Mayekawa Mfg Co Ltd | Method for utilizing cold and its device |
| CN2758674Y (en) * | 2004-12-23 | 2006-02-15 | 上海交通大学 | Refrigerating device for recovering liquefied natural gas cold energy for cold storage |
-
2006
- 2006-11-21 CN CNB2006101236638A patent/CN100424450C/en not_active Expired - Fee Related
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3724229A (en) * | 1971-02-25 | 1973-04-03 | Pacific Lighting Service Co | Combination liquefied natural gas expansion and desalination apparatus and method |
| US4329842A (en) * | 1980-07-02 | 1982-05-18 | Hans D. Linhardt | Power conversion system utilizing reversible energy of liquefied natural gas |
| JPH0926228A (en) * | 1995-07-07 | 1997-01-28 | Eibisu:Kk | Method for utilizing heat energy and cold energy contained in liquefied natural gas, and system for utilizing heat energy and cold energy contained in liquefied natural gas |
| CN1295646A (en) * | 1998-03-27 | 2001-05-16 | 埃克森美孚上游研究公司 | Producing power from pressurized liquefied natural gas |
| CN1342879A (en) * | 2000-09-13 | 2002-04-03 | 谢红飞 | Method for utilizing cold on gasifying liquefied natural gas |
| CN1447016A (en) * | 2002-03-22 | 2003-10-08 | 中国科学院工程热物理研究所 | Gas turbine generating system and flow by cooling liquefied natural gas to separate carbon dioxide |
| CN2602186Y (en) * | 2002-09-24 | 2004-02-04 | 中国科学技术大学 | Semiconductive temperature difference power generating and hydrogen production apparatus using cold energy of liquefied natural gas |
| JP2004211949A (en) * | 2002-12-27 | 2004-07-29 | Mayekawa Mfg Co Ltd | Method for utilizing cold and its device |
| CN2758674Y (en) * | 2004-12-23 | 2006-02-15 | 上海交通大学 | Refrigerating device for recovering liquefied natural gas cold energy for cold storage |
Non-Patent Citations (2)
| Title |
|---|
| LNG冷能利用及发展前景. 李静，李志红，华贲.加工利用与安全环保，第25卷第5期. 2005 |
| LNG冷能利用及发展前景. 李静，李志红，华贲.加工利用与安全环保，第25卷第5期. 2005 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1963347A (en) | 2007-05-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100424450C (en) | Method for using cooling capacity of LNG with cooling media as medium and apparatus thereof | |
| CN101551060B (en) | Method and device for integrated utilization of natural gas pipe network pressure energy refrigeration and hydrate | |
| CN101806293B (en) | Integrating and optimizing method for improving generation efficiency of liquefied natural gas cold energy | |
| CN105888742B (en) | Efficient liquid-air energy storage/release system | |
| CN202868298U (en) | Gradient utilization system of LNG (Liquefied Natural Gas) cold energy | |
| EP0683847B1 (en) | An improved liquefied natural gas fueled combined cycle power plant | |
| EP2753861B1 (en) | Method and apparatus for power storage | |
| CN101245956A (en) | Method for utilizing pressure energy of natural gas | |
| CN103267394A (en) | Method and device for efficiently utilizing cold energy of liquefied natural gas | |
| CN114216046B (en) | LNG cold energy and data center cold supply coupling system and method | |
| US20230241544A1 (en) | Integrated heat management systems and processes for adsorbed natural gas storage facilities | |
| CN104154416A (en) | Ice storage method and device comprising an atmospheric tower and utilizing cold energy of LNG | |
| CN206695421U (en) | LNG cold energy refrigerating circulatory devices | |
| CN108005739A (en) | Using the LNG cold energy stepped utilization methods of cold energy generation | |
| US20230138866A1 (en) | Energy storage device for water electrolysis hydrogen production coupled with low temperature and energy storage method | |
| CN204717343U (en) | A kind of refrigeration plant for reclaiming boil-off gas cold energy | |
| CN204827549U (en) | System is utilized to high efficiency that pipe network natural gas pressure energy and cold energy were retrieved | |
| CN107304974B (en) | Liquefied natural gas cold energy recovery system and method | |
| CN204477679U (en) | A kind of LNG warehouse BOG recycling system | |
| CN106839486A (en) | LNG cold energy cooling cycle systems | |
| CN205618981U (en) | Liquefied natural gas cold energy recovery system | |
| CN201628446U (en) | Recovery system for cold energy released in vaporization of cryogenic liquid | |
| CN216643796U (en) | LNG cold energy and data center cooling coupling system | |
| CN202485329U (en) | Methane liquefaction device for scattered air source points | |
| CN205714296U (en) | Natural gas gas storage well peak regulation energy conserving system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20081008 Termination date: 20111121 |