CN102538387A - Liquefied natural gas (LNG) low temperature liquefied three-level refrigeration spiral wound tube type heat exchanger - Google Patents
Liquefied natural gas (LNG) low temperature liquefied three-level refrigeration spiral wound tube type heat exchanger Download PDFInfo
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- CN102538387A CN102538387A CN2011103731109A CN201110373110A CN102538387A CN 102538387 A CN102538387 A CN 102538387A CN 2011103731109 A CN2011103731109 A CN 2011103731109A CN 201110373110 A CN201110373110 A CN 201110373110A CN 102538387 A CN102538387 A CN 102538387A
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Abstract
The invention belongs to the field of natural gas low temperature liquefied technology, and relates to a liquefied natural gas (LNG) three-level low temperature liquefied process device and a mixed refrigerant refrigeration technology, which cools 6.0MPa, -120DEG C natural gas into -164DEG C to be liquefied in two-steam spiral wound tube type heat exchanger by applying a certain proportion of non-azeotropic N2-CH4 mixed refrigerant, thereby being convenient for LNG to be stored in a surpercooling mode and being convenient to transport. The non-azeotropic N2-CH4 mixed refrigerant is firstly precooled and liquefied by a three-level refrigerant spiral wound tube type heat exchanger, and is throttled to a shell pass after being liquefied to cool a LNG tube bundle and a N2-CH4 mixed refrigerant precooling tube bundle from a secondary outlet in -120DEG C, thereby leading natural gas and precoolded refrigerant in the tube pass to be liquefied, and achieving the purpose of precooling mixed refrigerant before throttling and liquefying nature gas at low temperature. The LNG three-level low temperature liquefied process device is compact in structure and high in heat exchange efficiency, can be used to exchange heat for mixed gas with low-temperature phase transition, solves the difficult problem of LNG three-level low temperature technology, and increases low temperature heat exchange efficiency of a LNG system.
Description
Technical field
The invention belongs to natural gas in low temperature liquefaction technology field, relate to a kind of LNG three grade low-temp liquefaction process equipment and mix refrigerant Refrigeration Technique, use the non-azeotropic N of certain proportioning
2-CH
4Mix refrigerant is cooled to-164 ℃ and liquefaction with 6.0MPa ,-120 ℃ of natural gases in two plume spiral winding pipe formula heat exchangers, so that LNG crosses iced storage and convenient transportation.The cold spiral winding pipe formula of three tier structure heat exchanger is the precooling and the non-azeotropic N that liquefies at first
2-CH
4Be throttled into the shell side cooling behind the mix refrigerant, mix refrigerant liquefaction from the outlet temperature of secondary LNG tube bank and N for-120 ℃
2-CH
4Mix refrigerant precooling tube bank; Interior natural gas of tube side and precooling cold-producing medium all are liquefied, reach preceding precooling of mix refrigerant throttling and natural gas in low temperature liquefaction purpose, its compact conformation; Heat exchange efficiency is high; Can be used for mist band phase transformation low-temperature heat exchange, solve LNG three grade low-temp technical barriers, improve LNG system hypothermia heat exchange efficiency.
Background technology
Large-scale mix refrigerant natural gas liquefaction flow process mainly comprises three phases; First stage is that the natural gas after the compression is carried out precooling; Be about to 36 ℃ of natural gas precoolings to-53 ℃, second stage is that natural gas is cooled to-120 ℃ from-53 ℃, for low-temperature liquefaction is prepared; Three phases is that-120 ℃ of natural gases are cooled to-164 ℃ and liquefaction, and three processes can adopt different refrigeration process, different cold-producing medium and various heat exchange equipment.At present, the mix refrigerant natural gas liquefaction system adopts whole heat exchange mode mostly, and three sections process of refrigerastions are connected to an integral body; The heat exchanger height can reach 60～80 meters, and heat exchange efficiency is improved significantly, but the problem that exists is a too complicacy of heat-exchanging process flow process; The heat transmission equipment volume is too huge, gives processing and manufacturing, on-the-spot install and transportation brings serious inconvenience, and in case problem such as pipe leakage occurs; Be difficult to detect, be easy to cause whole heat exchanger to scrap, the set technique equipment stops production.In addition, because common tubular heat exchanger adopts tube sheet to connect the bundle of parallel tubes mode, simple in structure, the self-constriction ability is relatively poor, is generally the heat exchange of sub-thread stream, and heat exchange efficiency is lower, and volume is bigger, and the temperature difference is less, is difficult to natural gas is cooled off in a flow process and liquefies.The present invention is according to LNG three grade low-temps liquefaction characteristics, and independently spiral winding pipe formula heat exchanger is as main heat transmission equipment separately to adopt three sections, and the segmentation independent cooling is to third level N
2-CH
4The technological process of mix refrigerant low-temperature liquefaction; Third level low-temperature liquefaction technology and the equipment of primary study exploitation warm area between-120 ℃～-164 ℃; Solve third level natural gas in low temperature liquefaction core technology problem, promptly bifilar stream spiral winding pipe formula heat exchanger structure and technological process problem.
Summary of the invention
The present invention is primarily aimed at natural gas third level low-temperature liquefaction problem, adopts to have volume is little, heat exchange efficiency is high, heat transfer temperature difference is big, have self-tightening contraction adjustment function bifilar stream spiral winding pipe formula heat exchanger as main heat exchange equipment, uses non-azeotropic N
2-CH
4The refrigeration process flow process of throttling after the precooling of mix refrigerant elder generation, control freezing by change of state flow process, and then control natural gas liquefaction temperature and pressure improve heat exchange efficiency, solve natural gas three grade low-temps liquefaction problem.
Technical solution of the present invention:
The cold spiral winding pipe formula of LNG low-temperature liquefaction three tier structure heat exchange equipment; Comprise mix refrigerant outlet tube sheet 21 after mix refrigerant outlet bobbin carriage 20 after mix refrigerant outlet(discharge) flange 19 after mix refrigerant discharge connection 18 after LNG discharge connection 1, LNG outlet tube sheet 2, upper cover 3, mix refrigerant suction flange 4, mix refrigerant entrance sleeve 5, cylindrical shell 6, central tube 7, filler strip 8, natural gas helical bundle 9, mix refrigerant precooling tube bank 10, mix refrigerant precooling entrance sleeve 11, mix refrigerant precooling suction flange 12, mix refrigerant precooling import bobbin carriage 13, mix refrigerant precooling import tube sheet 14, mix refrigerant discharge connection 15, LNG outlet(discharge) flange 16, LNG outlet bobbin carriage 17, the precooling, the precooling, the precooling, the precooling, go up bracing ring 22, ear seat 23, bracing ring 24, natural gas entrance sleeve 25, natural gas suction flange 26, natural gas import bobbin carriage 27, natural gas import tube sheet 28, low head 29, mix refrigerant discharge connection flange 30 down; It is characterized in that: natural gas helical bundle 9, mix refrigerant precooling tube bank 10 are twined around central tube 7, and the tube core after the winding is installed in the cylindrical shell 6; Central tube 7 one ends are installed bracing ring 22; One end is installed bracing ring 24 down; Last bracing ring 22 is fixed in cylindrical shell 6 tops, and following bracing ring 24 is fixed in cylindrical shell 6 bottoms, and natural gas helical bundle 9, mix refrigerant precooling tube bank 10 are wound between bracing ring 22 and the following bracing ring 24; Cylindrical shell 6 tops are connected with end socket 3, and tube sheet 2 is installed at end socket 3 tops, and tube sheet 2 bottoms connect tube bank 9, and bobbin carriage 17 is installed at the top, and bobbin carriage 17 tops are installed and taken over 1, take over 1 top mounting flange 16; Cylindrical shell 6 bottoms are connected with end socket 29, and end socket 29 tops are installed refrigerant outlet and taken over 15, take over 15 top mounting flanges 30; Cylindrical shell 6 upper left-hand are installed refrigerant inlet and are taken over 5, and cold-producing medium precooling outlet tube sheet 21 is installed on the right side, and tube sheet 21 left sides connect mix refrigerant precooling tube bank 10 outlets, and the right side connects bobbin carriage 20; Cylindrical shell 6 lower left side are installed cold-producing medium precooling import tube sheet 14, and tube sheet 14 right sides connect the mix refrigerant precooling and restrain 10 imports, and the left side connects bobbin carriage 13; Natural gas import tube sheet 28 is installed on right side, cylindrical shell 6 bottom, and natural gas import tube sheet 28 left sides connect 9 imports of natural gas helical bundle, and the right side connects bobbin carriage 27; Cylindrical shell 6 middle part mounting ear seats 23.
N
2-CH
4Mix refrigerant gets into mix refrigerant precooling bobbin carriage 13 when-120 ℃ and 1.58MPa, in bobbin carriage 13, reallocate in mix refrigerant precooling tube bank 10 each arm, tube bank 10 after spiral twines in cylindrical shell 10 by the N after the throttling
2-CH
4Mix refrigerant precooling and liquefaction; Flow to bobbin carriage 20 after cold-producing medium liquefies fully, temperature is reduced to-164 ℃, pressure and is reduced to 1.38MPa, again through be installed on take over 18 with adapter 5 between the choke valve throttling; Pressure is reduced to 0.3MPa after the throttling; The nitrogen temperature becomes-185 ℃ after the throttling, is in the gas-liquid two-phase state, and methane temperature becomes-163.5 ℃ after the throttling; Be in supercooled liquid phase state; Mix refrigerant after the throttling is a gas-liquid two-phase, through take over 5 get into cylindrical shells 6 and the cooled natural gas helical bundle 9 that flows downward, precooling mix refrigerant tube bank 10 after ,-130 ℃, flow out the three tier structure device for cooling through taking over 15 during 0.3MPa.
Natural gas-120 ℃, get into natural gas import bobbin carriage 27 during 5.5MPa, in bobbin carriage 27, reallocate in natural gas helical bundle 9 each arm, tube bank 9 is twined the back in cylindrical shell 6 and the N after the throttling through spiral
2-CH
4Mix refrigerant carries out heat exchange, and temperature is reduced to-161 ℃, liquefy fully when pressure is reduced to 5.3MPa and cold excessively, crosses to flow to bobbin carriage 17 after cold, flows out the three tier structure device for cooling through taking over 1 again, sends into the LNG basin after the throttling step-down.
The problems of principle that scheme is related:
At first, traditional LNG mix refrigerant natural gas liquefaction system adopts whole heat exchange mode, adopts a complete refrigeration system, and heat exchange efficiency is significantly improved than tandem type LNG liquefaction system; Heat exchanger quantity is reduced, and whole liquefaction process flow process obtains simplifying, and the refrigeration system of independent operating reduces; Convenient management, but after the problem that exists is the liquefaction process process simplification, make the LNG main heat exchanger bulky; Heat-exchanging process is complicated, processing and manufacturing, on-the-spot install and transport difficulty increases, and in case problem such as pipe leakage occurs; Be difficult to detect, cause whole heat exchanger to scrap easily, the set technique equipment stops production.For addressing this problem; The present invention is divided into 36 ℃～-53 ℃ ,-53 ℃～-120 ℃ with natural gas temperature change procedure in the main heat exchanger;-120 ℃～-164 ℃ three ranks adopt three independently heat exchangers, accomplish three temperature ranges heat transfer process from high to low; The primary study exploitation third level-120 ℃～-164 ℃ of low-temperature heat exchange flow processs and third level heat exchanger general structures and import and export parameter, and adopt N
2-CH
4The mix refrigerant refrigeration process solves the 3rd section low-temperature liquefaction process equipment problem.Research process is relatively independent, can with preceding two sections be connected to become integral body, it is consistent with integrated main heat exchange heat exchange principle to connect the back, is convenient to main heat exchanger partition back and transports and installation.Secondly, adopt N
2-CH
4Behind the mix refrigerant refrigeration process, must carry out precooling and liquefaction to cold-producing medium before the throttling.The cryogen import is 1.58MPa ,-120 ℃ the time, N
2-CH
4Methane is liquefied in the mix refrigerant, and nitrogen does not reach capacity yet, is in gas phase state, when pressure reach 1.38MPa, when precooling temperature reaches-164 ℃, nitrogen reaches capacity and is liquefied, after the liquefaction again throttling can obtain bigger refrigerating capacity.Precooling process and natural gas liquefaction and cross cold process and carry out simultaneously, so, two plume low-temperature heat exchange processes must be adopted, and traditional tubular heat exchanger is owing to adopt two large tubesheets to connect the bundle of parallel tubes structures; Volume is bigger, and heat transfer temperature difference is less, is prone to subregion; Tube pitch is bigger, and the self-constriction ability is relatively poor, is generally the heat exchange of sub-thread stream; Heat exchange efficiency is lower, is difficult to natural gas is cooled off in a flow process and liquefies, and is difficult for accomplishing bifilar stream uniform heat exchange process.The present invention has developed the bifilar stream spiral winding pipe of the 9Ni steel formula cryogenic heat exchanger that can bear 6.4MPa pressure, low temperature-185 ℃, can accomplish bifilar stream heat transfer process under the high pressure low temperature operating mode.Adopt non-azeotropic N
2-CH
4Behind the mix refrigerant, can make the saturated liquid nitrogen throttling after the cryogen inlet temperature reach-185 ℃, produce enough heat transfer temperature difference motive forces.Simultaneously; Methane throttling under supercooled state can continue to utilize its sensible heat to-163.5 ℃ of supercooled states, evaporates during the temperature that reaches capacity-146 ℃ again; Make three grades of liquefaction process have three low-temperature heat exchange temperature; Comprise two evaporating temperatures, reduce the diabatic process entropy production, reduce the diabatic process loss with this.
Technical characterstic of the present invention:
The present invention is primarily aimed at the cold spiral winding pipe formula of LNG low-temperature liquefaction three tier structure heat exchange equipment; Employing has that volume is little, heat exchange efficiency is high, heat transfer temperature difference is big, have bifilar stream spiral winding pipe formula heat exchanger that self-tightening shrinks the adjustment function as main heat exchange equipment, uses non-azeotropic N
2-CH
4The refrigeration process flow process of throttling after the precooling of mix refrigerant elder generation, control freezing by change of state flow process, and then control natural gas liquefaction temperature and pressure; Improve heat exchange efficiency; Solve natural gas-120 ℃～-164 ℃ three grade low-temp refrigeration problem, make three grades of liquefaction process have three low-temperature heat exchange temperature, comprise two evaporating temperatures; Reduce the diabatic process entropy production with this, reduce the diabatic process loss; The cold process of three tier structure has compact conformation with spiral winding pipe formula heat exchanger; Multiple medium band phase-change heat transfer; Heat transfer coefficient is big, can solve three grades of mix refrigerant precoolings of natural gas, a natural gas in low temperature liquefaction technology difficult problem in the Large LNG low-temperature liquefaction process, improves system's heat exchange and liquefaction efficiency; After using three grades of LNG low-temperature liquefaction processes, the LNG main heat exchanger can be divided into three independently heat exchangers, and volume reduces; Sectional carries out processing and manufacturing, transportation and on-the-spot the installation; In case problems such as pipe leakage occur, be easy to detect, be difficult for causing whole heat exchanger to scrap and the stopping production of set technique equipment; But the thermic load of the cold spiral winding pipe formula of LNG low-temperature liquefaction three tier structure heat exchange equipment reasonable distribution liquefaction stages and super cooled sect; Liquefaction stages and super cooled sect are coordinated relatively; The load distribution and the heat exchanger tube strength characteristics that can combine super-huge heat exchanger; Adopt the mode of sectional center tube winding screw coil pipe, guarantee theoretically winding process evenly and intensity adhere to specification; Choose reasonable the method for heat exchanger inlet and outlet position and material, a plurality of tubule plate of employing side can make heat exchanger structure compact more, heat transfer process is optimized; Outer medium counter flow of spiral winding pipe formula Tube Sheet of Heat Exchanger and across are skimmed over winding pipe, and heat exchanger tube oppositely twines between heat exchanger layer and the layer, even Reynolds number is lower, it is the turbulent flow form still, and the coefficient of heat transfer is bigger; Owing to be multiple medium band phase-change heat-exchange process, less to pressure reduction between the different medium and temperature difference requirement for restriction, the process units operation easier reduces, and security is improved; Spiral winding pipe formula heat exchanger is high pressure resistant and sealing is reliable, thermal expansion can compensate voluntarily, is prone to realize Large LNG liquefaction operation.
Description of drawings
Shown in Figure 1 is the critical piece structure and the position relation of the cold spiral winding pipe formula of LNG low-temperature liquefaction three tier structure heat exchange equipment.
The specific embodiment
With the secondary outlet temperature be-120 ℃ natural gas line with take over 25 and be connected; Natural gas-120 ℃, get into natural gas import bobbin carriage 27 during 5.5MPa; In bobbin carriage 27, reallocate in natural gas helical bundle 9 each arm, tube bank 9 is twined the back in cylindrical shell 6 and the N after the throttling through spiral
2-CH
4Mix refrigerant carries out heat exchange, and temperature is reduced to-161 ℃, liquefy fully when pressure is reduced to 5.3MPa and cold excessively, crosses to flow to bobbin carriage 17 after cold; To take over 1 with after LNG level Four choke valve is connected, LNG flows out the three tier structure device for cooling through taking over 1, after level Four choke valve throttling step-down, sends into the LNG basin; Mix refrigerant pipeline before the precooling is connected N with adapter 11
2-CH
4Mix refrigerant gets into mix refrigerant precooling bobbin carriage 13 when-120 ℃ and 1.58MPa, in bobbin carriage 13, reallocate in mix refrigerant precooling tube bank 10 each arm, tube bank 10 after spiral twines in cylindrical shell 6 by the N after the throttling
2-CH
4Mix refrigerant precooling liquefaction flow to bobbin carriage 20 after cold-producing medium liquefies fully, and temperature is reduced to-164 ℃, pressure and is reduced to 1.38MPa; Mix refrigerant after the precooling is taken over 18 be connected N with choke valve
2-CH
4Mix refrigerant pressure after the choke valve throttling is reduced to 0.3MPa, and the nitrogen temperature becomes-185 ℃ after the throttling, is in the gas-liquid two-phase state, and methane temperature becomes-163.5 ℃ after the throttling, is in the liquid phase supercooled state; Mix refrigerant pipeline after the throttling connects takes over 5; Cold-producing medium is after taking over 5 entering cylindrical shells 6 and the cooled natural gas that flows downward tube bank 9, precooling mix refrigerant tube bank 10;-130 ℃, flow out the three tier structure device for cooling through taking over 15 during 0.3MPa, get into LNG two-stage system cooling system.
Claims (3)
1.LNG the cold spiral winding pipe formula of low-temperature liquefaction three tier structure heat exchange equipment; It is characterized in that: the cold spiral winding pipe formula of LNG low-temperature liquefaction three tier structure heat exchange equipment; Comprise mix refrigerant outlet tube sheet 21 after mix refrigerant outlet bobbin carriage 20 after mix refrigerant outlet(discharge) flange 19 after mix refrigerant discharge connection 18 after LNG discharge connection 1, LNG outlet tube sheet 2, upper cover 3, mix refrigerant suction flange 4, mix refrigerant entrance sleeve 5, cylindrical shell 6, central tube 7, filler strip 8, natural gas helical bundle 9, mix refrigerant precooling tube bank 10, mix refrigerant precooling entrance sleeve 11, mix refrigerant precooling suction flange 12, mix refrigerant precooling import bobbin carriage 13, mix refrigerant precooling import tube sheet 14, mix refrigerant discharge connection 15, LNG outlet(discharge) flange 16, LNG outlet bobbin carriage 17, the precooling, the precooling, the precooling, the precooling, go up bracing ring 22, ear seat 23, bracing ring 24, natural gas entrance sleeve 25, natural gas suction flange 26, natural gas import bobbin carriage 27, natural gas import tube sheet 28, low head 29, mix refrigerant discharge connection flange 30 down; It is characterized in that: natural gas helical bundle 9, mix refrigerant precooling tube bank 10 are twined around central tube 7, and the tube core after the winding is installed in the cylindrical shell 6; Central tube 7 one ends are installed bracing ring 22; One end is installed bracing ring 24 down; Last bracing ring 22 is fixed in cylindrical shell 6 tops, and following bracing ring 24 is fixed in cylindrical shell 6 bottoms, and natural gas helical bundle 9, mix refrigerant precooling tube bank 10 are wound between bracing ring 22 and the following bracing ring 24; Cylindrical shell 6 tops are connected with end socket 3, and tube sheet 2 is installed at end socket 3 tops, and tube sheet 2 bottoms connect tube bank 9, and bobbin carriage 17 is installed at the top, and bobbin carriage 17 tops are installed and taken over 1, take over 1 top mounting flange 16; Cylindrical shell 6 bottoms are connected with end socket 29, and end socket 29 tops are installed refrigerant outlet and taken over 15, take over 15 top mounting flanges 30; Cylindrical shell 6 upper left-hand are installed refrigerant inlet and are taken over 5, and cold-producing medium precooling outlet tube sheet 21 is installed on the right side, and tube sheet 21 left sides connect mix refrigerant precooling tube bank 10 outlets, and the right side connects bobbin carriage 20; Cylindrical shell 6 lower left side are installed cold-producing medium precooling import tube sheet 14, and tube sheet 14 right sides connect the mix refrigerant precooling and restrain 10 imports, and the left side connects bobbin carriage 13; Natural gas import tube sheet 28 is installed on right side, cylindrical shell 6 bottom, and natural gas import tube sheet 28 left sides connect 9 imports of natural gas helical bundle, and the right side connects bobbin carriage 27; Cylindrical shell 6 middle part mounting ear seats 23.
2. according to claim
1The cold spiral winding pipe formula of described LNG low-temperature liquefaction three tier structure heat exchange equipment is characterized in that: N
2-CH
4Mix refrigerant gets into mix refrigerant precooling bobbin carriage 13 when-120 ℃ and 1.58MPa, in bobbin carriage 13, reallocate in mix refrigerant precooling tube bank 10 each arm, tube bank 10 after spiral twines in cylindrical shell 6 by the N after the throttling
2-CH
4Mix refrigerant precooling liquefaction; Flow to bobbin carriage 20 after cold-producing medium liquefies fully, temperature is reduced to-164 ℃, pressure and is reduced to 1.38MPa, again through be installed on take over 18 with adapter 5 between the choke valve throttling; Pressure is reduced to 0.3MPa after the throttling; The nitrogen temperature becomes-185 ℃ after the throttling, is in the gas-liquid two-phase state, and methane temperature becomes-163.5 ℃ after the throttling; Be in the liquid phase supercooled state; Mix refrigerant is a gas-liquid two-phase after the throttling, through take over 5 get into cylindrical shells 6 and the cooled natural gas helical bundle 9 that flows downward, precooling mix refrigerant tube bank 10 after ,-130 ℃, flow out the three tier structure device for cooling through taking over 15 during 0.3MPa.
3. according to claim
1The cold spiral winding pipe formula of described LNG low-temperature liquefaction three tier structure heat exchange equipment; It is characterized in that: natural gas-120 ℃, get into natural gas import bobbin carriage 27 during 5.5MPa; In bobbin carriage 27, reallocate in natural gas helical bundle 9 each arm, tube bank 9 is twined the back in cylindrical shell 6 and the N after the throttling through spiral
2-CH
4Mix refrigerant carries out heat exchange, and temperature is reduced to-161 ℃, liquefy fully when pressure is reduced to 5.3MPa and cold excessively, crosses to flow to bobbin carriage 17 after cold, flows out the three tier structure device for cooling through taking over 1 again, sends into the LNG basin after the throttling step-down.
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Application publication date: 20120704 |