CN104315802A - Method and equipment for dynamically recycling evaporated gas of liquefied natural gas - Google Patents
Method and equipment for dynamically recycling evaporated gas of liquefied natural gas Download PDFInfo
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Abstract
The invention discloses a method and equipment for dynamically recycling evaporated gas of liquefied natural gas. The method includes firstly, monitoring density, temperature and pressure data of the evaporated gas of the liquefied natural gas stored in a storage tank; secondly, computing and preliminarily judging super-cooling quantities required by the liquefied natural gas stored in the storage tank according to the monitored data; thirdly, enabling propane media to be in refrigerating cycles and then inputting the super-cooling quantities into the liquefied natural gas stored in the storage tank via heat exchange; fourthly, enabling the liquefied natural gas in a super-cooling state to return the storage tank by means of circulation, enabling the liquefied natural gas in the storage tank to reach new super-cooling state balance, dissolving evaporated gas generated in the liquefied natural gas into the liquefied natural gas again and reducing evaporation quantities by 80%; fifthly, starting to execute the first step, the second step, the third step and the fourth step again when the evaporated gas of the liquefied natural gas stored in the storage tank is layered. The equipment comprises the liquefied natural gas storage tank, a low-temperature pump, a heat exchanger, a refrigerating plant, a sensor and a control device. The method and the equipment have the advantages that the evaporated gas of the liquefied natural gas can be dynamically recycled, and the equipment can run stably without being frequently started and stopped and is high in safety and low emission and operating cost.
Description
Technical field
The present invention relates to the pneumatic state recovery method of a kind of natural gas vaporization and equipment.
Background technology
Current coal, oil are mankind's major consumers energy, and in primary energy consumption structure, coal accounts for 68.5%, and oil accounts for 17.7%, and natural gas only accounts for 4.7%, the world average level far below 24%.This energy consumption structure based on coal can hide some dangers for atmospheric environment.Liquefied natural gas (LNG) is the Optimum storage form of natural gas, under the situation that current environmental requirement is increasingly serious, for the LNG industry of technology-intensive type, research and development LNG correlation technique, especially LNG stores correlation technique, has important Social benefit and economic benefit to the development of LNG industry.
LNG utilizes the metal storage tank of band anti-leak and heat insulation layer to store usually, is mainly divided into singly holds tank, double volume tank, full appearance tank and film tank according to the mechanics bearing mode for liquid and vapour seal system.Due to the heat input produced in external heat and operating process, the liquefied natural gas in storage tank constantly will produce boil-off gas.Existing LNG facility generally includes liquefaction again with directly outer defeated for the processing form of boil-off gas, and these two kinds of patterns all exist the drawback in application.The cold that low pressure LNG had that liquefied form is defeated beyond comprising again makes boil-off gas liquefy within the condenser again and adopts kind of refrigeration cycle to liquefy two kinds of forms again.These two kinds again liquefied form be all the direct process to boil-off gas (gaseous methane), the use prerequisite of condenser is that a large amount of gasification is outer defeated, this operating mode only the large-scale gasification station of extremely minority at comparatively high-load operation time can realize.Adopt kind of refrigeration cycle to be the deficiency that boil-off gas liquefies, the generation of boil-off gas is discontinuous, and this will cause the frequent start-stop of cryogenic compressor, and cryogenic compressor is expensive, make cost recovery to meet cost-effectiveness requirement.Defeated outside boil-off gas is direct exist pressure match difficulty, and the discontinuous frequent start-stop making compressor equally of boil-off gas generation, when without outer defeated demand, can only take a large amount of torch burning or cold emptying, makes discharge and cost increase, brings potential safety hazard simultaneously.
Therefore, ubiquitous boil-off gas process problem in current LNG storage and transport station, is necessary to change thinking, take LNG as cold input carrier, adopt a set of new recovery system, make the smooth operation of boil-off gas treatment system, with the security in satisfied operation and cost-effectiveness requirement.
Summary of the invention
Main purpose of the present invention is to solve existing natural gas vaporization gas recovery method above shortcomings part, and the pneumatic state recovery method of a kind of natural gas vaporization and equipment are provided, make natural gas vaporization pneumatic state recovery method have stable, without the need to the low effect of frequent start-stop, high safety and discharge capacity, and can not affect by the outer defeated working conditions change of natural gas vaporization gas gasification, operation cost significantly reduces.
The object of the invention is to be realized by following technical scheme:
The pneumatic state recovery method of natural gas vaporization of the present invention, is characterized in that: comprise the following steps,
(1) density of the boil-off gas of the liquefied natural gas stored in storage tank, temperature, pressure data are monitored;
(2) cold excessively needed for the liquefied natural gas stored in anticipation storage tank is calculated according to Monitoring Data;
(3) liquefied natural gas stored in storage tank by heat exchange after utilizing propane medium kind of refrigeration cycle continues input cold;
(4) liquefied natural gas of supercooled state is reached through being circulated back to storage tank inside, storage tank inner liquefied natural gas entirety reaches new supercooled state balance, the boil-off gas produced in liquefied natural gas is dissolved in liquefied natural gas again, and evaporation capacity can realize the reduction of 80% in this case;
(5) when signs of delamination appears in the boil-off gas of the liquefied natural gas stored in storage tank, (one) to (four) step is restarted.
The pneumatic state recovery method of aforesaid natural gas vaporization, wherein, in described (one) to the density of the evaporation capacity of the liquefied natural gas stored in storage tank, temperature, pressure data is monitored is completed by a sensor be arranged on storage tank inwall guide-rail sliding mechanism, measuring period is 30 minutes, and measurement category is the whole liquid level scope of storage tank; During measurement, the density of each liquid level point, temperature, pressure data feed back by sensor, calculated by control system synthesis, the refrigerating capacity of required input in anticipation storage tank, this demand is passed to control device with signal form by data wire simultaneously, control refrigerating plant by control device again and carry out the generation of execution cold, control cryogenic pump simultaneously and the liquefied natural gas with refrigerating capacity a great deal of is delivered in refrigerating plant and heat exchanger by inner extraction the out of storage tank;
Calculate according to Monitoring Data the liquefied natural gas that stores in anticipation storage tank in described (two) and cross cold needed for it, the density according to sensor passes, pressure, temperature signal, calculate the overall thermal mechanical state of liquefied natural gas in current storage tank and enthalpy entropy and the saturation state enthalpy entropy of contrast under routine operating pressure (18KPa) by control system, obtain the cold needing outside input;
The kind of refrigeration cycle of propane medium adopts propane to be the two-stage refrigeration circulation of medium in described (three), every grade of kind of refrigeration cycle is passed through by compressor, condenser, expander and evaporimeter connect successively after refrigerating plant realize recycling of propane medium, first order circulation realizes medium temperature and is reduced to subzero 60 DEG C, it is subzero 190 DEG C and enter in heat exchanger shell pass and carry out heat exchange with the liquefied natural gas in tube side that the second level realizes medium outlet temperature, LNG temperature is made to be reduced to subzero 175 to 180 DEG C, cross the thermodynamic state that cold increases to saturation state under routine operating pressure, the disposal ability of this refrigerating plant is 1 ton/hour, routine operating pressure is 18KPa,
The liquefied natural gas reaching supercooled state in described (four) is temperature is subzero 175 ± 10 DEG C, and the liquefied natural gas reaching supercooled state, by the pressure reduction between refrigerating plant and storage tank, gets back to storage tank inside;
The boil-off gas of the liquefied natural gas stored in storage tank in described (five) occurs that signs of delamination is that in 3m, the temperature difference reaches 10 DEG C, or in storage tank, pressure reaches 20KPa, or in 3m, density contrast reaches 3%.
The equipment that the pneumatic state recovery method of natural gas vaporization of the present invention uses, is characterized in that, comprise liquefied natural gas (LNG) storage tank 1, cryogenic pump 2, heat exchanger 3, refrigerating plant 4, sensor 5 and control device 6;
In liquefied natural gas (LNG) storage tank 1, top tank structure vertical direction is provided with guide rail, and rail height equals storage tank inner canister height, and guide rail is stainless steel 304 material; This guide rail is provided with sensor 5, sensor 5 is slided within the scope of whole liquid level elevation in storage tank and walks, and carry out kinetic measurement to data, 30 minutes measuring periods in moving in the vertical direction; Also the density of each liquid level point, temperature and pressure data are carried out COMPREHENSIVE CALCULATING, the refrigerating capacity of required input in anticipation storage tank, this refrigeration capacity requirement is passed to refrigerating plant with signal form by data wire simultaneously and carry out the generation of execution cold, pass to cryogenic pump simultaneously and the liquefied natural gas with refrigerating capacity a great deal of is delivered in refrigerating plant and heat exchanger by inner extraction the out of storage tank;
This cryogenic pump 2 is installed on pump barrel inside, and this pump barrel is that vertical configuration is fixed on storage tank 1 madial wall, and cryogenic pump 2 entrance is positioned at bottom pump barrel, pump barrel distance from bottom storage tank bottom surface 650 ± 10mm, and cryogenic pump outlet is positioned at storage tank 1 top and is connected with heat exchanger 3 entrance;
The outlet of this heat exchanger 3 is connected with the supercooled state Liquid natural gas inlet being arranged on storage tank 1 top by pipeline, returns in storage tank 1 by the liquefied natural gas reaching supercooled state by pressure differential; Heat exchanger 3 entrance is connected with external transport pipeline, and pipeline adopts 12 cun of stainless steel tubes;
This refrigerating plant 4 is followed in series to form by compressor, condenser, expander and evaporimeter; This compressor inlet is connected with evaporimeter propane outlets pipeline, and compressor outlet is connected with condenser inlet; This condensator outlet is connected with expander import; This expander outlet is connected with evaporator; This evaporator outlet is connected with the import of heat exchanger 3 shell side by refrigeration propane medium pipeloop; Send into heat exchanger continuously to realize refrigeration propane medium cold is passed to liquefied natural gas, then get back to the continuous circulation in refrigerating plant;
This cryogenic pump 2, heat exchanger 3, refrigerating plant 4 and sensor 5 are connected with control device respectively.
The equipment that the pneumatic state recovery method of aforesaid natural gas vaporization uses, wherein, described storage tank 1 adopts full appearance formula structure, Inner tank adopts 304 stainless steels or 9 nickel steel materials to make, hold liquified natural gas and its boil-off gas, the ultralow temperature of resistance to subzero 175 ± 10 DEG C, Inner tank outer wrap resilient felt, resilient felt outer layer covers perlite cold insulation material, this perlite cold insulation material outer setting prestressed concrete external wall structure, operating pressure is 18 to 25KPa, and guide rail is arranged on interior top tank structure, along the vertical layout of tank height;
The vertical movement that described sensor 5 is realized on guide rail by electronic slip mechanism, this slide mechanism is single track slide block type mechanism, and this single track slide block type mechanism employing material is the single track slide block type mechanism of SS304, and model is SRS15WMUU; Sensor is bolted on the slide block of slide mechanism, and slide mechanism is connected with control device, and its sliding frequency is redefined for the stroke completing once the full liquid level measurement of higher degree for 1 hour; The data that sensor 5 monitors in each position are passed to control device, then control cryogenic pump, heat exchanger 3 and refrigerating plant 4 respectively by control device and carry out work; This sensor 5 adopts the form of temperature, pressure, density continuous measurement, pressure, temperature, the density value of the evaporation capacity of liquefied natural gas in real time dynamic measurement storage tank, tracking calculating after measuring-signal being received by control device, determine boil-off gas generation and current residing operating mode, and control signal is passed to cryogenic pump 2, heat exchanger 3 and refrigerating plant 4 by control device;
Described cryogenic pump 2 adopts major axis to dive liquid centrifugal multistage pump multiple centrifugal pump, its stainless steel pump barrel is that vertical configuration is fixed on storage tank 1 inwall, and storage tank 1 top is fixed on pump barrel top, and pump barrel bottom extends to storage tank minimum operation liquid level place, pump barrel internal diameter is 32 cun, wall thickness 8mm, material is 304 stainless steels, and this storage tank minimum operation liquid level is 650mm, operating pressure 1MPa, flow 120 tons/hour, installs bottom valve bottom pump barrel, and this bottom valve controls entering of liquefied natural gas; Cryogenic pump 2 outlet is positioned at storage tank top and is connected with one end of external transport pipeline by check valve, and the external transport pipeline other end is connected with heat exchanger entrance, and the liquified natural gas extracted out by cryogenic pump is delivered to heat exchanger tube pass entrance; The light data wire of cryogenic pump 2 through being connected with storage tank inner sensor receives the control signal sent here by sensor, calculate liquefied natural gas in storage tank and reach refrigerating capacity under operating pressure needed for poised state, liquified natural gas with refrigerating capacity a great deal of is extracted out by storage tank inside, and delivers to heat exchanger 3 import by 12 cun of stainless steel external transport pipelines that storage tank top is stretched out;
Described heat exchanger 3 adopts tube shell type structure, and operating pressure is 0.6MPa, and heat exchanger tube pass and shell side adopt 304 stainless steels to make, and is LNG in tube side, and be propane liquid in shell side, the LNG reaching supercooled state after heat exchange utilizes pressure differential to send back in storage tank by outlet; Heat exchanger 3 exports and is connected with carrying the one end reaching supercooled state LNG pipeline, and this conveying reaches the other end of supercooled state LNG pipeline and storage tank top supercooled state Liquid natural gas inlet passes through Flange joint; This pipeline is 12 cun of stainless steel pipeloops;
Described control device model is 854ATG.
Beneficial effect of the present invention: the pneumatic state recovery method of natural gas vaporization of the present invention take LNG as cold input carrier, adopt the method for dynamic calculation demand in carrier, to continue to carry out cold using propane as refrigerant by two-stage refrigeration circulation and input to dissolve unnecessary boil-off gas and the recovery method reducing evaporation rate, make the smooth operation of boil-off gas processing procedure, realize operation security economy, effectively can be applied in all kinds of middle-size and small-size liquefied natural gas receiving station, Storage, peak regulation station and Fen Shu satellite station etc., it has stable, without the need to frequent start-stop, high safety, discharge capacity is low, effect that outside the pale of civilization defeated working conditions change of not being bullied impact and operation cost significantly reduce, also can reduce the generation of boil-off gas, avoid the generation of overpressure alarm and cold and hot air defense, decrease torch burning waste, reduce CO2 emission, environmental, moreover its device structure is reasonable in design, convenient operation.
Accompanying drawing explanation
Fig. 1 is natural gas vaporization of the present invention pneumatic state reclaimer structural representation.
Major label description in figure:
1 liquefied natural gas storage tank, 2 cryogenic pumps, 3 heat exchangers, 4 refrigerating plants, 5 sensors, 6 control device.
Detailed description of the invention
Below in conjunction with accompanying drawing, the invention will be further described.
As shown in Figure 1, the pneumatic state recovery method of natural gas vaporization and equipment, liquefied natural gas storage tank 1, cryogenic pump 2, heat exchanger 3, refrigerating plant 4, sensor device 5, control device 6.Storage tank 1 adopts full appearance formula structure, Inner tank adopts 304 stainless steels or 9 nickel steel materials to make, hold liquified natural gas and its boil-off gas, the ultralow temperature of resistance to-162 degrees Celsius, outer wrap resilient felt and perlite cold insulation material, most external adopts prestressed concrete external wall structure, operating pressure 18-25KPa, sensor 5 adopts RTD form, the pressure of real time dynamic measurement storage tank medium, temperature, density value, by calculating the tracking of measuring-signal, determine boil-off gas generation and current residing operating mode, and control signal is passed to cryogenic pump 2, cryogenic pump adopts major axis to dive liquid centrifugal multistage pump multiple centrifugal pump form, storage tank top is fixed on by stainless steel pump barrel, pump barrel extends to minimum operation liquid level by storage tank top always, its minimum operation liquid level is 650mm, operating pressure 1MPa, flow 120 tons/hour, feed liquor is controlled by by the bottom valve installed bottom pump barrel.Cryogenic pump receives the control signal sent here by sensor, and the liquid LNG of specified amount packets of information contained extracts out, and the 12 cun of stainless steel external transport pipelines stretched out by storage tank top deliver to heat exchanger 3, and end adopts Flange joint, and flange and pipeline adopt 300 pounds of levels.Refrigerating plant 4 comprises propane compressor, expander, condenser and evaporimeter, adopt bipolar kind of refrigeration cycle, medium is reduced to subzero 60 degrees Celsius by the first order, medium propane continues to be reduced to-190 degrees Celsius by the second level, low temperature refrigerant propane after the liquid LNG sent by cryogenic pump and refrigerating plant process carries out heat exchange, heat exchanging process completes in heat exchanger 3, heat exchanger adopts tube shell type structure, operating pressure is 0.6MPa, internals adopt 304 stainless steels to make, be LNG in tube side, be propane liquid in shell side, the LNG reaching supercooled state after heat exchange utilizes pressure differential to send back in storage tank by outlet.Dynamic Execution said process, LNG after deep cooling is increased the solubility of gaseous methane, reduce boil-off gas cause storage tank internal pressure too high and rolling risk, directly subzero treatment is carried out for LNG and avoids the interruption of liquefaction process and frequent start-stop, make stable operation.
Embodiment one:
For certain medium-sized liquefied natural gas peak regulation station, the outer defeated production capacity 800,000 tons of year gaseous state, 80,000 side's low temperature LNG storage tank one is set, gasify during peak regulation outer throughput rate 200 tons/hour, within 160 days, calculate according to annual work, according to conventional way of recycling, the direct losses caused by evaporation loss about 4000 tons of liquefied natural gas, in addition, because the frequent start-stop during peak regulation and boil-off gas reclaim the impact of the vibration brought for structure and internals, to extra internals replacing, repair and maintenance work etc. be caused, overall calculation year economic loss about 1,200 ten thousand yuan.
Transform according to the pneumatic state recovery method of natural gas vaporization of the present invention and equipment, fix vertical sensor installation guide rail in 80,000 side's storage tank inside by top, guide rail is made with stainless steel 304 material, is fixed on storage tank inwall, and height is equal with inner canister height; This guide rail arranges slide mechanism, and this slide mechanism selects single track slide block type mechanism, and this single track slide block type mechanism employing material is the single track slide block type mechanism of SS304, and model is SRS15WMUU; Sensor is bolted on the slide block of slide mechanism, and slide mechanism is connected with control device, and its sliding frequency is redefined for the stroke completing once the full liquid level measurement of higher degree for 1 hour; Sensor vertically can be movably walking and realize density, pressure, temperature within the scope of the interior full liquid level of kinetic measurement storage tank, kinetic measurement is carried out to data, 30 minutes measuring periods.Occur that in 3m, the temperature difference reaches 10 DEG C when storing in storage tank, or pressure reaches 20KPa in storage tank, or after in 3m, the density contrast any one reached in 3% occurs, calculate the overall thermal mechanical state of liquefied natural gas in current storage tank, with the saturation state comparison under operating pressure (18KPa), calculate the cold value of required input in anticipation storage tank, the data that cold numerical value is passed back by sensor are determined after control device calculates, be decided by working condition requirement at that time, finally make to make boil-off gas to be again dissolved in liquified natural gas after input cold.Demand for cold passes to refrigerating plant with signal form by data wire and carries out performing cold and generate, pass to cryogenic pump simultaneously and delivered in kind of refrigeration cycle and heat exchanger by the liquefied natural gas of a great deal of.As calculated, be about 0.5 ton/hour, outer defeated pressure for the outer quantitative requirement of cryogenic pump, cryogenic pump to send to the LNG temperature of heat exchanger entrance about subzero 158 DEG C, boil-off gas mean temperature about 158 degrees Celsius in storage tank simultaneously, pressure 22KPa.Liquefied natural gas delivers to heat exchanger tube pass through cryogenic pump and 12 cun of external transport pipelines.Be propane liquid in shell side, and by condensed in two stages device, expander, evaporimeter, realize recycling of propane medium, first order circulation realizes medium temperature and reduces subzero 60 DEG C, the second level realizes subzero 190 DEG C and enter in heat exchanger shell pass and carry out heat exchange with the liquefied natural gas in tube side of medium outlet temperature, make LNG temperature be reduced to subzero 178 DEG C, the liquefied natural gas this being reached supercooled state, by the pressure reduction between refrigerating plant and storage tank, gets back to storage tank inside; Cross cold natural gas vaporization rate and reduce by 80%, the LNG after deep cooling increases the solubility of gaseous methane, makes pressure in storage tank be down to 18KPa by 22KPa.
After transforming, after adopting the inventive method liquid towards LNG to freeze, the disadvantage of conventional solution can be eliminated completely, cost-saving about 1,000 ten thousand yuan of year.
The content be not described in the present embodiment is prior art, therefore no longer repeats.
Advantage of the present invention: by the compressor in refrigerating plant 4, expander, condenser and evaporimeter, realize recycling of refrigerant propane, first order kind of refrigeration cycle realizes medium temperature and reduces subzero about 60 DEG C, second level kind of refrigeration cycle realizes subzero about 190 DEG C and enter in heat exchanger shell pass and carry out heat exchange with the liquefied natural gas in tube side of medium outlet temperature, LNG temperature is made to be reduced to subzero 175 DEG C to 180 DEG C, cross cold and increase to predetermined extent, heat exchange is completed in the liquid LNG sent by cryogenic pump and the low temperature refrigerant propane heat exchanger 3 after refrigerating plant process.Dynamic Execution said process, LNG after deep cooling is increased the solubility of boil-off gas (gaseous state first), reduce the too high and rolling risk of the storage tank internal pressure that causes of boil-off gas, directly carrying out subzero treatment to LNG avoids the interruption of liquefaction process and frequent start-stop, makes operating process more stable.
The advantage of the pneumatic state recovery method of natural gas vaporization of the present invention and equipment is, provide a kind of based on to the dynamic monitoring of natural gas vaporization rate in low temperature (subzero 175 ± 10 DEG C) storage tank and anticipation, and then utilize refrigerant to carry out the input of dynamic continuance cold to it, ensure boil-off gas recovery method and the equipment of storage tank internal pressure stabilises, it adopts sensor to internal tank temperature, pressure, density signal continues to monitor, utilize media collapse, condensation, expand, the kind of refrigeration cycle of evaporation, by cryogenic media and liquefied natural gas heat exchange, cold energy is imported, the cold of crossing of liquefied natural gas increases, the solubility of the gaseous methane in reservoir vessel in liquid state is made to remain on higher degree, reduce the generation of boil-off gas, avoid the generation of overpressure alarm and cold and hot air defense, decrease torch burning waste, reduce CO2 emission and operation cost, can be applicable to all kinds of middle-size and small-size gasification station, Fen Shu satellite station and storage vault.
The above, it is only preferred embodiment of the present invention, not any pro forma restriction is done to the present invention, every above embodiment is done according to technical spirit of the present invention any simple modification, equivalent variations and modification, all still belong in the scope of technical solution of the present invention.
Claims (4)
1. the pneumatic state recovery method of natural gas vaporization, is characterized in that: comprise the following steps,
(1) density of the boil-off gas of the liquefied natural gas stored in storage tank, temperature, pressure data are monitored;
(2) cold excessively needed for the liquefied natural gas stored in anticipation storage tank is calculated according to Monitoring Data;
(3) liquefied natural gas stored in storage tank by heat exchange after utilizing propane medium kind of refrigeration cycle continues input cold;
(4) liquefied natural gas of supercooled state is reached through being circulated back to storage tank inside, storage tank inner liquefied natural gas entirety reaches new supercooled state balance, the boil-off gas produced in liquefied natural gas is dissolved in liquefied natural gas again, and evaporation capacity can realize the reduction of 80% in this case;
(5) when signs of delamination appears in the boil-off gas of the liquefied natural gas stored in storage tank, (one) to (four) step is restarted.
2. the pneumatic state recovery method of natural gas vaporization according to claim 1, it is characterized in that, in described (one) to the density of the evaporation capacity of the liquefied natural gas stored in storage tank, temperature, pressure data is monitored is completed by a sensor be arranged on storage tank inwall guide-rail sliding mechanism, measuring period is 30 minutes, and measurement category is the whole liquid level scope of storage tank; During measurement, the density of each liquid level point, temperature, pressure data feed back by sensor, calculated by control system synthesis, the refrigerating capacity of required input in anticipation storage tank, this demand is passed to control device with signal form by data wire simultaneously, control refrigerating plant by control device again and carry out the generation of execution cold, control cryogenic pump simultaneously and the liquefied natural gas with refrigerating capacity a great deal of is delivered in refrigerating plant and heat exchanger by inner extraction the out of storage tank;
Calculate according to Monitoring Data the liquefied natural gas that stores in anticipation storage tank in described (two) and cross cold needed for it, the density according to sensor passes, pressure, temperature signal, calculate the overall thermal mechanical state of liquefied natural gas in current storage tank and enthalpy entropy and the saturation state enthalpy entropy of contrast under routine operating pressure (18KPa) by control system, obtain the cold needing outside input;
The kind of refrigeration cycle of propane medium adopts propane to be the two-stage refrigeration circulation of medium in described (three), every grade of kind of refrigeration cycle is passed through by compressor, condenser, expander and evaporimeter connect successively after refrigerating plant realize recycling of propane medium, first order circulation realizes medium temperature and is reduced to subzero 60 DEG C, it is subzero 190 DEG C and enter in heat exchanger shell pass and carry out heat exchange with the liquefied natural gas in tube side that the second level realizes medium outlet temperature, LNG temperature is made to be reduced to subzero 175 to 180 DEG C, cross the thermodynamic state that cold increases to saturation state under routine operating pressure, the disposal ability of this refrigerating plant is 1 ton/hour, routine operating pressure is 18KPa,
The liquefied natural gas reaching supercooled state in described (four) is temperature is subzero 175 ± 10 DEG C, and the liquefied natural gas reaching supercooled state, by the pressure reduction between refrigerating plant and storage tank, gets back to storage tank inside;
The boil-off gas of the liquefied natural gas stored in storage tank in described (five) occurs that signs of delamination is that in 3m, the temperature difference reaches 10 DEG C, or in storage tank, pressure reaches 20KPa, or in 3m, density contrast reaches 3%.
3. an equipment for the pneumatic state recovery method use of natural gas vaporization as claimed in claim 1, is characterized in that, comprise liquefied natural gas storage tank 1, cryogenic pump 2, heat exchanger 3, refrigerating plant 4, sensor 5 and control device 6;
In liquefied natural gas storage tank 1, top tank structure vertical direction is provided with guide rail, and rail height equals storage tank inner canister height; This guide rail is provided with sensor 5;
This cryogenic pump 2 is installed on pump barrel inside, and this pump barrel is that vertical configuration is fixed on storage tank 1 madial wall, and cryogenic pump 2 entrance is positioned at bottom pump barrel, pump barrel distance from bottom storage tank bottom surface 650 ± 10mm, and cryogenic pump outlet is positioned at storage tank 1 top and is connected with heat exchanger 3 entrance;
The outlet of this heat exchanger 3 is connected with the supercooled state Liquid natural gas inlet being arranged on storage tank 1 top by pipeline, returns in storage tank 1 by the liquefied natural gas reaching supercooled state by pressure differential; Heat exchanger 3 entrance is connected with external transport pipeline;
This refrigerating plant 4 is followed in series to form by compressor, condenser, expander and evaporimeter; This compressor inlet is connected with evaporimeter propane outlets pipeline, and compressor outlet is connected with condenser inlet; This condensator outlet is connected with expander import; This expander outlet is connected with evaporator; This evaporator outlet is connected with the import of heat exchanger 3 shell side by refrigeration propane medium pipeloop;
This cryogenic pump 2, heat exchanger 3, refrigerating plant 4 and sensor 5 are connected with control device respectively.
4. the equipment of the pneumatic state recovery method use of natural gas vaporization according to claim 3, it is characterized in that, described storage tank 1 adopts full appearance formula structure, Inner tank adopts 304 stainless steels or 9 nickel steel materials to make, Inner tank outer wrap resilient felt, resilient felt outer layer covers perlite cold insulation material, this perlite cold insulation material outer setting prestressed concrete external wall structure, operating pressure is 18 to 25KPa, and guide rail is arranged on interior top tank structure, along the vertical layout of tank height;
The vertical movement that described sensor 5 is realized on guide rail by electronic slip mechanism, this slide mechanism is single track slide block type mechanism, sensor is bolted on the slide block of slide mechanism, slide mechanism is connected with control device, and its sliding frequency is redefined for the stroke completing once the full liquid level measurement of higher degree for 1 hour;
Described cryogenic pump 2 adopts major axis to dive liquid centrifugal multistage pump multiple centrifugal pump, its stainless steel pump barrel is that vertical configuration is fixed on storage tank 1 inwall, and storage tank 1 top is fixed on pump barrel top, and pump barrel bottom extends to storage tank minimum operation liquid level place, install bottom valve bottom pump barrel, this bottom valve controls entering of liquefied natural gas; Cryogenic pump 2 outlet is positioned at storage tank top and is connected with one end of external transport pipeline by (12 cun) check valve, and the external transport pipeline other end is connected with heat exchanger entrance, and the liquified natural gas extracted out by cryogenic pump is delivered to heat exchanger tube pass entrance;
Described heat exchanger 3 adopts tube shell type structure, operating pressure is 0.6MPa, heat exchanger tube pass and shell side adopt 304 stainless steels to make, be LNG in tube side, be propane liquid in shell side, heat exchanger 3 exports and is connected with carrying the one end reaching supercooled state LNG pipeline, and this conveying reaches the other end of supercooled state LNG pipeline and storage tank top supercooled state Liquid natural gas inlet passes through Flange joint;
Described control device model is 854ATG.
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| CN105398548A (en) * | 2015-11-12 | 2016-03-16 | 中远船务工程集团有限公司 | Working ship group with natural gas liquefaction, storage, transportation and regasification functions |
| CN106524665A (en) * | 2015-09-14 | 2017-03-22 | 安瑞科(廊坊)能源装备集成有限公司 | Liquefaction and recovery device and method of LNG container evaporation gas |
| WO2018203011A1 (en) * | 2017-05-05 | 2018-11-08 | Gaztransport Et Technigaz | Storage facility for a liquefied gas |
| CN111649229A (en) * | 2019-03-25 | 2020-09-11 | 沪东中华造船(集团)有限公司 | LNG filling vessel filling system and LNG filling vessel cabin pressure control method |
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| CN106524665A (en) * | 2015-09-14 | 2017-03-22 | 安瑞科(廊坊)能源装备集成有限公司 | Liquefaction and recovery device and method of LNG container evaporation gas |
| CN105398548A (en) * | 2015-11-12 | 2016-03-16 | 中远船务工程集团有限公司 | Working ship group with natural gas liquefaction, storage, transportation and regasification functions |
| CN109219720A (en) * | 2017-05-05 | 2019-01-15 | 气体运输技术公司 | storage device for liquefied gas |
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| WO2018203011A1 (en) * | 2017-05-05 | 2018-11-08 | Gaztransport Et Technigaz | Storage facility for a liquefied gas |
| KR20200004236A (en) * | 2017-05-05 | 2020-01-13 | 가즈트랑스포르 에 떼끄니가즈 | Storage equipment for liquefied gas |
| RU2770338C2 (en) * | 2017-05-05 | 2022-04-15 | Газтранспорт Эт Технигаз | Plant for liquefied gas storage |
| CN109219720B (en) * | 2017-05-05 | 2023-02-17 | 气体运输技术公司 | Storage device for liquefied gas |
| KR102579882B1 (en) * | 2017-05-05 | 2023-09-19 | 가즈트랑스포르 에 떼끄니가즈 | Storage facilities for liquefied gas |
| CN111649229A (en) * | 2019-03-25 | 2020-09-11 | 沪东中华造船(集团)有限公司 | LNG filling vessel filling system and LNG filling vessel cabin pressure control method |
| CN113154797A (en) * | 2020-01-23 | 2021-07-23 | 气体产品与化学公司 | System and method for recondensing boil-off gas from a liquefied natural gas tank |
| CN113154797B (en) * | 2020-01-23 | 2022-11-11 | 气体产品与化学公司 | System and method for recondensing boil-off gas from a liquefied natural gas tank |
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