CN104034122A - System and method for re-condensing boil off gas (BOG) of liquefied natural gas - Google Patents
System and method for re-condensing boil off gas (BOG) of liquefied natural gas Download PDFInfo
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Abstract
The invention discloses a system and a method for re-condensing a boil off gas (BOG) of a liquefied natural gas. The system comprises a liquefied natural gas storage device, a BOG re-condensing device and a liquefied natural gas conveying device, wherein the BOG re-condensing device comprises a static mixer and a gas-liquid separator, an outlet in the top of the gas-liquid separator is connected with a BOG main pipe of a liquefied natural gas storage tank, an outlet in the bottom of the gas-liquid separator is connected with a liquefied natural gas low-pressure outward conveying main pipe, one end of the static mixer is connected with the gas-liquid separator, the other end of the static mixer is connected with the liquefied natural gas low-pressure outward conveying main pipe, and the BOG main pipe is sequentially connected with a compressor and a heat exchanger to be connected with the static mixer. The method includes mixing the liquefied natural gas and the BOG in the static mixer, then feeding the liquefied natural gas and the BOG into the gas-liquid separator, returning a separated gas to the BOG main pipe, and feeding a separated liquid phase into a booster pump outside the tank. According to the system and the method for re-condensing the BOG of the liquefied natural gas, by means of a static mixing and condensation manner, condensation efficiency of the BOG is increased, energy consumption is reduced, and purposes of saving equipment investment and facilitating system operation and maintenance are achieved.
Description
Technical field
The present invention relates to liquefied natural gas and store and induction system field, furtherly, relate to a kind of natural gas vaporization gas condenser system and method again.
Background technology
Liquefied natural gas (LNG) is a kind of high-grade energy, has the advantages that calorific value is high, Air-pollution From Combustion is little.The major function of LNG receiving station is to receive the LNG that transport by sea Ship Transportation is come, and it is stored and is gasified, to obtain gaseous natural gas (NG) product, and by gas distributing system to city dweller and (or) industrial user's air feed.
In the production process of LNG receiving station, because storage tank, pipeline, equipment etc. are from various factors such as environment heat absorption and the flash distillation of unloading a ship, atmospheric pressure changes, at LNG, store and transportation system can discharge a certain amount of boil-off gas (BOG) from LNG.If BOG deals with improperly, will cause low-temperature storage tank superpressure and cause danger, if outer row's burning will cause the waste of resource, meanwhile, also brought potential safety hazard and problem of environmental pollution, from the angle of energy-saving and emission-reduction, consider it is also worthless.Therefore the important topic that, how safely and effectively treatments B OGShi LNG receiving station must face.
Generally, the BOG of LNG receiving station adopts condensation method again to process, and this method compares that direct method (LNG direct weighting outer defeated) is safer, economy, environmental protection, therefore, is worldwide widely adopted.
As shown in Figure 1, during traditional industry is produced, the BOG of LNG receiving station again condenser system mainly comprises other conduit assemblies such as low-lift pump 102 in LNG storage tank 101, LNG tank, after-condenser 103, the outer booster pump 104 of LNG tank, BOG compressor 105, BOG compressor outlet heat exchanger 106, gasifier 107, torch 108.In Fig. 1, the BOG producing in LNG storage tank enters 105 pressurizations of BOG compressor by boil-off gas house steward, then enters after-condenser 103 after 106 heat exchange of BOG compressor outlet heat exchanger.LNG in LNG storage tank 101 has certain degree of supercooling after by 102 superchargings of low-lift pump in tank, part LNG enters after-condenser and BOG carries out heat exchange in after-condenser 103, another part LNG enters the outer booster pump 104 of tank with isolated liquid in after-condenser after mixing, after supercharging, enter gasifier 107 gasifications, then by the outer defeated house steward of liquefied natural gas high pressure, be delivered to downstream gas distributing system.
After-condenser is the nucleus equipment of traditional B OG recondensation process system, as shown in Figure 2.This after-condenser 103 comprises tank shell 201, be positioned at tank enclosure and be positioned at the liquid distribution trough 202 that LNG that LNG feed tube below makes to flow to its upper surface is evenly distributed, be positioned at distributor below filling the filling batch 203 of filler, be positioned at the vortex broken device 204 of after-condenser bottom.
On after-condenser top-side LNG entrance pipe, be provided with valve E; On the pipeline that after-condenser top is communicated with house steward BOG, be provided with valve F; On after-condenser tonifying Qi pipeline, be provided with valve G, on BOG compressor outlet heat exchanger low-temperature receiver pipeline, be provided with valve H.
In after-condenser 103, because the factors such as change of LNG storage tank operation operating mode all can cause the variation of BOG amount, this just needs to control the amount that enters the LNG in BOG after-condenser, can, by the whole condensations of all BOG, guaranteeing the safety of mixed liquor output channel and upstream device.Due to the variation of BOG and LNG amount, in after-condenser, air pressure can fluctuate, and in after-condenser, liquid level also can present labile state.When liquid level is following lower than the surface of filling batch 203, will affect the condensation by mixing speed of LNG and BOG, likely can make the LNG of after-condenser outlet at bottom pipeline output present nearly saturation state, if there is the impact (as ambient air temperature rising etc.) of extraneous other factors, LNG will gasify again, thereby causes " cavitation " of the outer booster pump 104 of downstream LNG tank.
The control system of after-condenser 103 as shown in Figure 2.
When the BOG pressure in after-condenser 103 increases, pressure controller C by-pass valve control F opens, and the BOG in 103 is disposed to house steward BOG.Fluid level controller G can monitor the liquid level of after-condenser, and controls by the aperture of valve G the gas flow that after-condenser tonifying Qi pipeline enters.When the liquid level in after-condenser raises, valve G opens, and inflates, thereby reduce the liquid level in after-condenser in after-condenser.The pressure of after-condenser, the LNG flow that enters after-condenser and the BOG temperature after BOG compressor heat exchanger and flow information are transferred to and in logical-arithmetic unit B, are carried out logical operation computing by pressure transmitter C, flow transmitter A, temperature transmitter E, flow transmitter D respectively, and by the aperture of by-pass valve control E, BOG is all cooling in after-condenser.The control that enters the gas temperature of after-condenser is realized by changing the aperture of valve H by temperature controller F.
This after-condenser intraware (as Pall ring, separator, deflector, internal pipeline etc.) complexity, logic control is more complicated.And because the condensing mode in after-condenser is taked Static Contact formula, therefore, condensation efficiency is lower, be conventionally the highlyest about 58%.On the other hand, existing recondensation process has the shortcomings such as energy consumption is relatively high, equipment investment is large, maintenance is inconvenient to a certain extent.
Summary of the invention
For solving problems of the prior art, the invention provides a kind of natural gas vaporization gas condenser system and method again.By adopting static mixing condensing mode, to improve BOG condensation efficiency, reduce energy consumption, and reach saving equipment investment, be convenient to the object of system Operation and maintenance.
One of object of the present invention is to provide a kind of natural gas vaporization gas condenser system again.
Comprise: liquefied natural gas storage device, boil-off gas be condensing unit and liquefied natural gas conveying device again, described liquefied natural gas storage device comprises LNG tank; Described liquefied natural gas conveying device comprises low-lift pump in LNG tank, the outer booster pump of tank and gasifier; LNG tank top is provided with two pipelines, and one is boil-off gas house steward, and another is torch house steward; In tank, low-lift pump is connected to the outer booster pump of tank by the outer defeated house steward of liquefied natural gas low pressure;
Described boil-off gas again condensing unit comprises static mixer and gas-liquid separator; Gas-liquid separator top exit connects the boil-off gas house steward of LNG tank, and gas-liquid separator outlet at bottom is connected to the outer defeated house steward of liquefied natural gas low pressure;
Static mixer one end connects gas-liquid separator, and the other end connects the outer defeated house steward of liquefied natural gas low pressure;
Boil-off gas house steward connects after compressor and heat exchanger successively, connects static mixer;
The outer booster pump outlet of tank connects the outer defeated house steward of liquefaction natural gas high pressure, and pipeline is divided into two, pipeline a and pipeline b, and pipeline a is connected gasifier after merging with pipeline b after heat exchanger;
Between gas-liquid separator top exit pipeline and gasifier export pipeline, by gas-liquid separator tonifying Qi pipeline, connect.
On gas-liquid separator top exit pipeline, be provided with valve A; On gas-liquid separator outlet at bottom pipeline, be provided with valve B;
On the pipeline that the outer defeated house steward of liquefied natural gas low pressure is connected with static mixer one end, be provided with valve C; On gas-liquid separator tonifying Qi pipeline, be provided with valve D.
Described static mixer can be one or more, can be in parallel or the form of series connection.
Particularly, described system can comprise:
(1) LNG stocking system, LNG storage tank and corresponding building block thereof;
(2) LNG condenser system again, mainly comprises following relevant device:
(a) house steward BOG, is connected with LNG storage tank, from LNG tank top, draws.
(b) BOG compressor, is arranged on LNG storage tank BOG gas phase pipeline, for BOG is pressurizeed;
(c) BOG compressor outlet heat exchanger, is arranged on BOG compressor outlet downstream, for reducing the temperature of BOG compressor outlet gas;
(d) static mixer, after being arranged on BOG compressor outlet heat exchanger and between gas-liquid separator, for the mixing of LNG and BOG;
(e) gas-liquid separator, is arranged on static mixer downstream, for separating of the gas-liquid two-phase medium that may exist in the static mixer port of export, prevents the outer booster pump " cavitation " of downstream LNG tank;
(f) LNG goes to static mixing pipeline, and one end is connected with static mixer, and the other end is connected on the outer defeated house steward of LNG storage tank;
(g) by-pass valve control and control instrument, be arranged on described BOG again on condenser system pipeline.
(3) the outer communication system of LNG, mainly comprises following relevant device:
(a) low-lift pump in LNG tank, for by LNG supercharging, makes it have certain degree of supercooling;
(b) the outer booster pump of LNG tank, for outer defeated by LNG supercharging;
(c) gasifier, for gasifying LNG;
(d) pipeline and building block thereof.
Two of object of the present invention is to provide a kind of natural gas vaporization gas condensation method again.
Comprise:
Liquefied natural gas and boil-off gas enter gas-liquid separator after mixing in static mixer, and isolated gas returns to boil-off gas house steward; Isolated liquid phase enters the outer booster pump of tank.
Specifically comprise the following steps:
1) the compressed heat exchange of boil-off gas that produces in LNG tank is laggard enters static mixer, and the liquefied natural gas in LNG tank enters static mixer by low-lift pump supercharging in tank is laggard;
2) liquefied natural gas and boil-off gas are carried out abundant heat exchange in static mixer, and the fluid after mixed heat transfer enters gas-liquid separator;
3) gas-liquid separator separates gas is out back to boil-off gas house steward, after the liquefied natural gas in the outer defeated house steward of isolated liquid phase and low pressure converges, enters the outer booster pump of tank, after supercharging, gasification, enters downstream gas distributing system.
Wherein,
The liquid level of gas-liquid separator is controlled by valve B; Liquid level is relevant to the outer high-pressure pump entrance height of tank and pressure controlling value;
The gas-phase space pressure at gas-liquid separator top is controlled by valve A and valve D; Pressure is controlled at 0.1～2MPag.
The degree of condensation of boil-off gas in static mixer controlled by valve C.Aperture by control valve C changes the LNG flow that enters static mixer, further controls the temperature in static mixer, realizes the total condensation of BOG.The medium temperature of static mixer outlet than this medium outside tank under high-pressure pump inlet pressure corresponding saturation temperature low 0～30 spend.
The present invention can be achieved through the following technical solutions:
The BOG producing in LNG storage tank enters BOG compressor pressurizes by house steward BOG, then enters static mixer entrance end through heat exchanger heat exchange is laggard.LNG in storage tank has certain degree of supercooling after by low-lift pump supercharging in LNG tank, part LNG enters static mixer by the pipeline that defeated house steward picks out outside low pressure and BOG carries out abundant heat exchange in static mixer, make BOG total condensation, fluid after mixed heat transfer enters gas-liquid separator and carries out gas-liquid separation, the gas of separating is back to house steward BOG, and the liquid of separating enters booster pump outside tank through defeated low-pressure manifold outside pipeline is back to LNG and with defeated LNG outside another part after mixing.LNG, after supercharging, enters that gasifier heat exchange gasification is laggard enters downstream gas distributing system, is delivered to resident and (or) industrial user.
In the present invention, can adopt the static mixer of arbitrary form.For example can adopt inner vanes is the static mixer that left-right rotary alternate cycle distributes, but is not limited to this kind of form.In general, this equipment adopts low temperature resistant, stainless steel.Static mixer two ends generally can adopt flange connect or be welded to connect.
In the present invention, the degree of condensation of BOG in static mixer realizes by the valve opening of controlling on the LNG pipeline being connected with static mixer arrival end.The valve opening that the liquid level of gas-liquid separator is controlled by controlling on the LNG export pipeline being connected with gas-liquid separator bottom realizes.The gas-phase space pressure at gas-liquid separator top is realized by the valve opening the tonifying Qi pipeline of controlling the valve opening on the pipeline being connected with separator top and returning from natural gas output.
Tool of the present invention has the following advantages:
1. adopt static mixer and the form of gas-liquid separator combination to carry out the condensation again of BOG, equipment simply and safety, condensation efficiency high.
On the one hand, static mixer and gas-liquid separator are common device, simple in structure, and than after-condenser, it is examined, maintenance operation is more convenient.On the other hand, consider the particular design of static mixer internal structure, its inner vanes can impel BOG to form a large amount of micro-bubbles, gas meter area increases greatly, effectively increase the area contacting with the LNG that enters static mixer, promoted heat exchange, thereby effectively improved condensation efficiency.
2. in the present invention, the BOG amount LNG stocking system not being produced limits, by regulating the LNG mixing with it to measure to reach the effect of total condensation in static mixer.In addition, the pressure of the liquid level of gas-liquid separator and top gas-phase space is controlled, more common in petrochemical production process, and control program is simple, safety and reliable.Therefore, the control program of the condensing plant again in the present invention is simple, reliable.
Above-mentioned all advantages make the present invention compare with traditional BOG recondensation process method, have higher economic benefit, lower comprehensive energy consumption, and be conducive to the Operation and maintenance of system.
Accompanying drawing explanation
Fig. 1 prior art BOG is condenser system schematic diagram again
Fig. 2 prior art BOG is the control program figure of BOG after-condenser in condenser system again
Fig. 3 BOG of the present invention is condenser system schematic diagram again
Fig. 4 BOG of the present invention is the control program figure of static mixer and gas-liquid separator in condenser system again
Description of reference numerals:
101LNG storage tank; Low-lift pump in 102LNG tank; 103 after-condensers; The outer booster pump of 104LNG tank; 105BOG compressor; 106BOG compressor outlet heat exchanger; 107 gasifiers; 108 torches; 109 static mixers; 110 gas-liquid separators
201 tank shells; 202 liquid distribution troughs; 203 filling batch; Vortex broken device 204
301 flow transmitter A; 302 logical-arithmetic unit B; 303 pressure controller C; 304 flow transmitter D; 305 temperature transmitter E; 306 temperature controller F; 307 fluid level controller G
401 pressure transmitter H; 402 temperature transmitter I; 403 fluid level controller J; 404 flow transmitter K; 405 temperature transmitter L; 406 logical-arithmetic unit M; 407 flow transmitter N; 408 temperature transmitter O; 409 flow controller P
501 valve A; 502 valve B; 503 valve C; 504 valve D; 505 valve E; 506 valve F; 507 valve G; 508 valve H
The specific embodiment
Below in conjunction with embodiment, further illustrate the present invention.
Embodiment:
As shown in Figure 3, the BOG of liquefied natural gas receiving station again condenser system mainly comprise low-lift pump 102 in LNG storage tank 101, LNG tank, the outer booster pump 104 of LNG tank, BOG compressor 105, BOG compressor outlet heat exchanger 106, gasifier 107, torch 108, static mixer 109, gas-liquid separator 110.The BOG producing in storage tank enters BOG compressor 105 pressurization by boil-off gas house steward, then enters static mixer 109 through heat exchanger 106 heat exchange are laggard.LNG in storage tank has certain degree of supercooling after by 102 superchargings of low-lift pump in tank, and a part of LNG enters static mixer 109 and carries out heat exchange with BOG.Fluid after mixed heat transfer enters in gas-liquid separator 110 and carries out gas-liquid separation, and the gas of separating is back to house steward BOG, and the liquid of separating is back to the outer defeated house steward of LNG low pressure, and enters the outer booster pump 104 of tank after mixing with the outer defeated LNG of another part.LNG, after supercharging, enters downstream gas distributing system by the outer defeated house steward of liquefied natural gas high pressure after entering gasifier 107 heat exchange and gasification, is delivered to resident and (or) industrial user.
In static mixer 109, because the factors such as change of LNG storage tank 101 operation operating modes all can cause the variation of BOG amount, this just needs to control LNG amount that enter in static mixer, can, by the whole condensations of all BOG, guaranteeing the safety of upstream device.Due to the variation of BOG and LNG amount, in gas-liquid separator, air pressure can fluctuate, and the liquid level in gas-liquid separator also can present labile state.When liquid level changes, may affect the pressure stability of outer booster pump 104 entrances of LNG tank, in order to guarantee the operation stability of pump, need to control accordingly the liquid level of gas-liquid separator 109 and top gas-phase space pressure, pressure is controlled at 0.77MPag, the medium temperature of static mixer outlet than this medium outside tank under high-pressure pump inlet pressure corresponding saturation temperature low 2 spend.
Static mixer in the present invention and the control system of gas-liquid separator are as shown in Figure 4.
Fluid temperature signal in the flow of the flow of the BOG of static mixer 109 arrival ends and temperature signal, LNG and temperature signal and gas-liquid separator 110 is transferred to and in logical-arithmetic unit M406, is carried out logical operation by flow transmitter K404, temperature transmitter L405, flow transmitter N407, temperature transmitter O408, temperature transmitter I402 respectively, calculate the required LNG amount of condensation BOG, and the regulation that is transferred to flow controller P409 by-pass valve control C503 enters the LNG flow of blender, realize whole condensations again of BOG.Fluid level controller J403 can monitor the liquid level in gas-liquid separator 110, and controls LNG output quantity by valve B502.
When in gas-liquid separator 110, pressure increases, pressure transmitter H401, by the aperture of by-pass valve control A501, is disposed to system house steward BOG by the BOG in gas-liquid separator.During pressure decreased in gas-liquid separation, valve D504 opens, and inflates, thereby increase the gas-phase space pressure in gas-liquid separator in gas-liquid separator.The method can realize the pressure stability of gas-liquid separator top gas-phase space.When the liquid level in gas-liquid separator changes, the aperture of fluid level controller J403 by-pass valve control B502, the flow of the liquefied natural gas of regulation output, realizes the stable of liquid level in gas-liquid separator.
Claims (6)
1. a natural gas vaporization gas condenser system again, comprising: liquefied natural gas storage device, boil-off gas be condensing unit and liquefied natural gas conveying device again, and described liquefied natural gas storage device comprises LNG tank; Described liquefied natural gas conveying device comprises low-lift pump in liquified natural gas tank, the outer booster pump of tank and gasifier; LNG tank top is provided with two pipelines, and one is boil-off gas house steward, and another is torch house steward; In tank, low-lift pump is connected to the outer booster pump of tank by the outer defeated house steward of liquefied natural gas low pressure, it is characterized in that:
Described boil-off gas again condensing unit comprises static mixer and gas-liquid separator; Gas-liquid separator top exit connects the boil-off gas house steward of LNG tank, and gas-liquid separator outlet at bottom is connected to the outer defeated house steward of liquefied natural gas low pressure;
Static mixer one end connects gas-liquid separator, and the other end connects the outer defeated house steward of liquefied natural gas low pressure;
Boil-off gas house steward connects after compressor and heat exchanger successively, connects static mixer;
The outer booster pump outlet of tank connects the outer defeated house steward of liquefaction natural gas high pressure, and pipeline is divided into two, pipeline a and pipeline b, and pipeline a is connected gasifier after merging with pipeline b after heat exchanger;
Between gas-liquid separator top exit pipeline and gasifier export pipeline, by gas-liquid separator tonifying Qi pipeline, connect.
2. natural gas vaporization gas as claimed in claim 1 condenser system again, is characterized in that:
On gas-liquid separator top exit pipeline, be provided with valve A; On gas-liquid separator outlet at bottom pipeline, be provided with valve B;
On the pipeline that the outer defeated house steward of liquefied natural gas low pressure is connected with static mixer one end, be provided with valve C; On gas-liquid separator tonifying Qi pipeline, be provided with valve D.
3. natural gas vaporization gas as claimed in claim 1 condenser system again, is characterized in that:
Described static mixer is parallel connection or series connection many.
4. the natural gas vaporization gas of employing as described in one of claim 1～3 condensation method again for condenser system again, is characterized in that described method comprises:
Liquefied natural gas and boil-off gas enter gas-liquid separator after mixing in static mixer, and isolated gas returns to boil-off gas house steward; After converging, liquefied natural gas in the outer defeated house steward of isolated liquid phase and low pressure enters the outer booster pump of tank.
5. the natural gas vaporization gas as claimed in claim 4 method of condensation again, is characterized in that described method comprises:
1) the compressed heat exchange of boil-off gas that produces in LNG tank is laggard enters static mixer, and the liquefied natural gas in LNG tank enters static mixer by low-lift pump supercharging in tank is laggard;
2) liquefied natural gas and boil-off gas are carried out abundant heat exchange in static mixer, and the fluid after mixed heat transfer enters gas-liquid separator;
3) gas-liquid separator separates gas is out back to boil-off gas house steward, after the liquefied natural gas in the outer defeated house steward of isolated liquid phase and low pressure converges, enters the outer booster pump of tank, after supercharging, gasification, enters downstream gas distributing system.
6. the natural gas vaporization gas as claimed in claim 5 method of condensation again, is characterized in that:
The liquid level of gas-liquid separator is controlled by valve B;
The gas-phase space pressure at gas-liquid separator top is controlled by valve A and valve D, and pressure is controlled at 0.1～2MPag;
The degree of condensation of boil-off gas in static mixer controlled by valve C;
The medium temperature of static mixer outlet than this medium outside tank under high-pressure pump inlet pressure corresponding saturation temperature low 0～30 spend.
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| CN111678276A (en) * | 2020-05-29 | 2020-09-18 | 北京中能航科科技有限公司 | Gas cooling method for performance test board of refrigeration compressor |
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