CN102538388B - Three-stream spiral wound type heat exchange equipment for secondary refrigeration and low-temperature liquefaction of LNG (liquefied natural gas) - Google Patents

Three-stream spiral wound type heat exchange equipment for secondary refrigeration and low-temperature liquefaction of LNG (liquefied natural gas) Download PDF

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CN102538388B
CN102538388B CN201110376419.3A CN201110376419A CN102538388B CN 102538388 B CN102538388 B CN 102538388B CN 201110376419 A CN201110376419 A CN 201110376419A CN 102538388 B CN102538388 B CN 102538388B
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outlet
import
bobbin carriage
gas
flange
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CN102538388A (en
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张周卫
汪雅红
张小卫
万续
鲁小军
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Abstract

The invention belongs to the technical field of low-temperature natural gas liquefaction, and relates to LNG (liquefied natural gas) secondary low-temperature liquefaction equipment and the technique of refrigeration by mixed refrigerant. C2H4 refrigerant and N2-CH4 mixed refrigerant steam of 0.3MPa and -130 DEG C from an LNG three-level outlet are used for cooling and liquefying natural gas of 5.8MPa and -53 DEG C in a three-stream spiral wound type heat exchanger, so that LNG can conveniently enter a three-level undercooling stage. The three-stream spiral wound type heat exchanger for secondary liquefaction is used for undercooling the C2H4 refrigerant first, the undercooled C2H4 refrigerant is throttled to a shell side to be mixed with the N2-CH4 to cool a -53-DEG C LNG pipeline, a N2-CH4 precooling tube bundle and a C2H4 undercooling tube bundle, so that undercooling of the C2H4 and precooling of the N2-CH4 and liquefaction of natural gas are realized. The equipment is compact in structure and high in heat exchange efficiency, and can be used for the field of phase-variable low-temperature heat exchange of gas at temperature ranging from -53 DEG C to -120 DEG C, the problem of LNG secondary low-temperature liquefaction is solved, and low-temperature heat exchanging efficiency of an LNG system can be improved.

Description

The LNG low-temperature liquefaction secondary three plume spiral winding pipe type heat exchange equipments that freeze
Technical field
The invention belongs to natural gas in low temperature liquefaction technology field, relate to LNG secondary low-temperature liquefaction equipment and mix refrigerant Refrigeration Technique, application C 2h 4cold-producing medium and LNG secondary import 0.3MPa, the N of-130 ℃ 2-CH 4mixed refrigerant vapor is cooled to-120 ℃ and liquefaction by 5.8MPa ,-53 ℃ of natural gases in three plume spiral winding tube type heat exchangers, so that LNG enters three grades of super cooled sects; Secondary freeze three plume spiral winding tube type heat exchangers first cross cold C 2h 4cold-producing medium, C 2h 4cross after cold and be throttled into shell side and N 2-CH 4cooling-53 ℃ of LNG tube banks, N from one-level after mixing 2-CH 4pre-cooler tube bundle and C 2h 4supercooling tube bundle, makes natural gas and N in tube side 2-CH 4middle CH 4liquefaction, reached cold C 2h 4, precooling N 2-CH 4and liquefied natural gas object; Its compact conformation, heat exchange efficiency is high, can be used for-53 ℃～-120 ℃ gas band phase transformation low-temperature heat exchanges, solves a LNG secondary low-temperature liquefaction difficult problem, improves 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 compression is carried out to precooling, be about to 36 ℃ of natural gases and be chilled in advance-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, mix refrigerant natural gas liquefaction system adopts overall heat exchange mode mostly, and three sections of process of refrigerastions are connected to an entirety, and heat exchanger height can reach 60～80 meters, heat exchange efficiency is improved significantly, but it is too complicated that the problem existing is heat-exchanging process flow process, and heat transmission equipment volume is too huge, bring serious inconvenience to processing and manufacturing, on-the-spot installation and transportation, once and there is the problems such as pipe leakage, be difficult to detect, be easy to cause whole heat exchanger to scrap, set technique equipment stops production.In addition, because common tubular heat exchanger adopts tube sheet, connect bundle of parallel tubes mode, simple in structure, self-constriction ability is poor, is generally the heat exchange of sub-thread stream, and heat exchange efficiency is lower, and volume is larger, and the temperature difference is less, is difficult to natural gas cooling and liquefaction in a flow process.The present invention is according to LNG secondary low-temperature liquefaction feature, and independently spiral winding tube type heat exchanger is as main heat transmission equipment separately to adopt three sections, and segmentation independent cooling, for second level C 2h 4cold-producing medium refrigeration process flow process, second level low-temperature liquefaction technology and the equipment of primary study exploitation warm area between-53 ℃～-120 ℃, solve second level natural gas in low temperature liquefaction Key technique problem, i.e. the LNG low-temperature liquefaction secondary three plume spiral winding tube type heat exchanger structure &processes flow process problems of freezing.
Summary of the invention
The present invention is mainly for natural gas secondary-53 ℃～-120 ℃ of low-temperature liquefaction problems, adopts to have that volume is little, heat exchange efficiency is high, heat transfer temperature difference is large, have self-tightening shrinks the three plume spiral winding tube type heat exchangers of adjusting function as main heat exchange equipment, applies C 2h 4after the first precooling of cold-producing medium, the refrigeration process flow process of throttling, controls freezing by change of state flow process, and then controls natural gas liquefaction temperature and pressure, improves heat exchange efficiency, solves natural gas secondary low-temperature liquefaction problem.
Technical solution of the present invention:
The LNG low-temperature liquefaction secondary three plume spiral winding pipe type heat exchange equipments that freeze, comprise N 2-CH 4shell side suction flange 1, N 2-CH 4shell side entrance sleeve 2, C 2h 4outlet(discharge) flange 3, C 2h 4discharge connection 4, C 2h 4 outlet bobbin carriage 5, C 2h 4 outlet tube sheet 6, N 2-CH 4outlet(discharge) flange 7, N 2-CH 4discharge connection 8, N 2-CH 4 outlet bobbin carriage 9, N 2-CH 4 outlet tube sheet 10, N 2-CH 4 outlet tube bank 11, cylindrical shell 12, spiral coil 13, lower support circle 14, N 2-CH 4 import tube bank 15, N 2-CH 4 import tube sheet 16, N 2-CH 4 import bobbin carriage 17, N 2-CH 4suction flange 18, N 2-CH 4entrance sleeve 19, C 2h 4 import tube bank 20, C 2h 4-N 2-CH 4mixed gas outlet adapter 21, C 2h 4-N 2-CH 4mixed gas outlet flange 22, low head 23, C 2h 4suction flange 24, C 2h 4entrance sleeve 25, C 2h 4 import bobbin carriage 26, C 2h 4 import tube sheet 27, Imported gas flange 28, Imported gas adapter 29, Imported gas bobbin carriage 30, Imported gas tube sheet 31, Imported gas tube bank 32, central tube 33, filler strip 34, ear seat 35, upper bracing ring 36, C 2h 4c after precooling outlet tube bank 37, gas outlet tube bank 38, gas outlet bobbin carriage 39, gas outlet adapter 40, gas outlet flange 41, gas outlet tube sheet 42, throttling 2h 4c after entrance sleeve 43, throttling 2h 4suction flange 44, upper cover 45, is characterized in that: Imported gas tube bank 32, N 2-CH 4 import tube bank 15, C 2h 4 import tube bank 20 is wound around around central tube 33, and the tube core after winding is installed in cylindrical shell 12; Bracing ring 36 is installed in central tube 33 one end, and lower support circle 14 is installed in one end, and upper bracing ring 36 is fixed on cylindrical shell 12 tops, and lower support circle 14 is fixed on cylindrical shell 12 bottoms, Imported gas tube bank 32, N 2-CH 4 import tube bank 15, C 2h 4 import tube bank 20 is wound between bracing ring 36 and lower support circle 14; Cylindrical shell 12 tops are connected with upper cover 45, and N is installed at upper cover 45 tops 2-CH 4shell side entrance sleeve 2 and N 2-CH 4shell side suction flange 1; Cylindrical shell 12 bottoms are connected with low head 23, and C is installed at low head 23 tops 2h 4-N 2-CH 4mixed gas outlet adapter 21 and C 2h 4-N 2-CH 4mixed gas outlet flange 22; Cylindrical shell 12 upper left-hand are installed N 2-CH 4 outlet tube sheet 10, N 2-CH 4 outlet tube sheet 10 right sides connect N 2-CH 4 outlet tube bank 11, left side connects N 2-CH 4 outlet bobbin carriage 9, N 2-CH 4 outlet bobbin carriage 9 tops connect N 2-CH 4discharge connection 8 and N 2-CH 4outlet(discharge) flange 7; Cylindrical shell 12 upper right are installed gas outlet tube sheet 42, gas outlet tube sheet 42 left sides connect gas outlet tube bank 38, right side connects gas outlet bobbin carriage 39, and gas outlet bobbin carriage 39 tops connect gas outlet adapter 40 and gas outlet flange 41; In the middle of cylindrical shell 12 tops, C is installed in below 2h 4 outlet tube sheet 6, C 2h 4 outlet tube sheet 6 is installed C above 2h 4precooling outlet tube bank 37, after C is installed 2h 4 outlet bobbin carriage 5, C 2h 4c is installed at outlet bobbin carriage 5 tops 2h 4discharge connection 4 and C 2h 4outlet(discharge) flange 3; C after cylindrical shell 12 top middle upper parts installation throttlings 2h 4c after entrance sleeve 43, throttling 2h 4suction flange 44; Cylindrical shell 12 lower left side are installed N 2-CH 4 import tube sheet 16, N 2-CH 4 import tube sheet 16 right sides connect N 2-CH 415 imports are restrained in import, and left side connects N 2-CH 4 import bobbin carriage 17, N 2-CH 4n is installed at import bobbin carriage 17 tops 2-CH 4entrance sleeve 19 and N 2-CH 4suction flange 18; Imported gas tube sheet 31 is installed on cylindrical shell 12 right sides, bottom, Imported gas tube sheet 31 left sides connect Imported gas and restrain 32 imports, right side connects Imported gas bobbin carriage 30, and Imported gas adapter 29 and Imported gas flange 28 are installed in Imported gas bobbin carriage 30 tops; Cylindrical shell is installed C in the middle of 12 bottoms 2h 4 import tube sheet 27, C 2h 4 import tube sheet 27 is installed C above 2h 4 import tube bank 20, after C is installed 2h 4 import bobbin carriage 26, C 2h 4c is installed at import bobbin carriage 26 tops 2h 4entrance sleeve 25 and C 2h 4suction flange 24; Cylindrical shell 12 middle part mounting ear seats 35.
C 2h 4cold-producing medium-53 ℃, enter C during 1.88MPa 2h 4import bobbin carriage 26, at C 2h 4in import bobbin carriage 26, be allocated in C 2h 420 each arms, C are restrained in import 2h 4 import tube bank 20 is interior by the C after throttling at cylindrical shell 12 after spiral winding 2h 4, from N 2-CH 4shell side entrance sleeve 2 enters the N of housing-130 ℃, 0.3MPa 2-CH 4mix refrigerant is excessively cold, and temperature is reduced to-120 ℃, pressure decreased to 1.58MPa, then flow to C 2h 4 outlet bobbin carriage 5, through being installed on C 2h 4c after discharge connection 4 and throttling 2h 4choke valve throttling between entrance sleeve 43 is subcooled liquid, and after throttling, Pressure Drop is to 0.3MPa, and temperature becomes-119.4 ℃, then after throttling C 2h 4entrance sleeve 43 enter cylindrical shell 12 with from three grades from N 2-CH 4shell side entrance sleeve 2 enters the N of housing 2-CH 4mix refrigerant mixes, the cooled natural gas import that flows downward after mixing tube bank 32, N 2-CH 4 import tube bank 15, C 2h 4after import tube bank 20 ,-63 ℃, during 0.3MPa through C 2h 4-N 2-CH 4mixed gas outlet is taken over 21 and is flowed out two-stage system device for cooling and enter one-level refrigerating section.
N 2-CH 4mix refrigerant-53 ℃, enter N during 1.88MPa 2-CH 4 import bobbin carriage 17, at N 2-CH 4in import bobbin carriage 17, be allocated in N 2-CH 415 each arms, N are restrained in import 2-CH 4 import tube bank 15 is interior by the C after throttling at cylindrical shell 12 after spiral winding 2h 4, from N 2-CH 4shell side entrance sleeve 2 enters the N of housing 2-CH 4mix refrigerant precooling, CH after precooling 4be liquefied and form N 2-CH 4biphase gas and liquid flow, temperature is reduced to-120 ℃, pressure decreased to 1.58MPa, then flow to N 2-CH 4 outlet bobbin carriage 9, through N 2-CH 4after discharge connection 8, enter the precooling of three tier structure device for cooling.
Natural gas-53 ℃, enter Imported gas bobbin carriage 30 during 5.8MPa, in Imported gas bobbin carriage 30, be allocated in Imported gas and restrain 32 each arms, Imported gas tube bank 32 C cylindrical shell 12 in and after throttling after spiral winding 2h 4, from N 2-CH 4shell side entrance sleeve 2 enters the N of housing 2-CH 4mix refrigerant carries out heat exchange, and temperature liquefies while being down to-120 ℃, Pressure Drop to 5.5MPa, flow to gas outlet bobbin carriage 39 after liquefaction, then through gas outlet, takes over 40 and flow out two-stage system device for cooling and enter three tier structure device for cooling.
The Principle Problems that scheme is related:
First, traditional LNG mix refrigerant natural gas liquefaction system adopts overall heat exchange mode, adopt a complete refrigeration system, heat exchange efficiency is significantly improved compared with tandem type LNG liquefaction system, heat exchanger quantity is reduced, entirety LNG Lquified Process Flow is simplified, the refrigeration system of independent operating reduces, convenient management, but after the problem existing is LNG Lquified Process Flow simplification, make LNG main heat exchanger bulky, heat-exchanging process complexity, processing and manufacturing, on-the-spot installation and transport difficulty increase, once and there is the problems such as pipe leakage, be difficult to detect, easily cause whole heat exchanger to scrap, set technique equipment stops production.For addressing this problem, the present invention is divided into 36 ℃～-53 ℃ ,-53 ℃～-120 ℃ by natural gas temperature change procedure in main heat exchanger,-120 ℃～-164 ℃ three ranks, adopt three independently heat exchangers, complete three temperature ranges heat transfer process from high to low, the primary study exploitation second level-53 ℃～-120 ℃ of low-temperature heat exchange flow processs and second level heat exchanger general structures and import and export parameter, and adopt C 2h 4cold-producing medium refrigeration process, solves second segment low-temperature liquefaction process equipment problem.Research process is relatively independent, can be connected to become entirety with two sections of front and back, consistent with integrated main heat exchange heat exchange principle after connecting, and is convenient to transport and install after main heat exchanger partition.Secondly, adopt C 2h 4after cold-producing medium refrigeration process, must be to C before throttling 2h 4carried out cold.Cryogen import is 1.88MPa ,-53 ℃ time, C 2h 4in liquid phase state, when pressure reaches 1.58MPa, temperature and reaches-120 ℃, C 2h 4cross cold and there is larger sensible heat, then can obtain larger refrigerating capacity after throttling.N 2-CH 4mix refrigerant is mainly used in the cold process of three tier structure, must be through-53 ℃～-120 ℃ ,-120 ℃～-164 ℃ two sections of low temperature precooling process before throttling, and in secondary process of refrigerastion, N 2-CH 4mix refrigerant precooling process and natural gas liquefaction and C 2h 4cross cold process and carry out simultaneously, so, three plume low-temperature heat exchange processes must be adopted.Traditional tubular heat exchanger is owing to having adopted two large tubesheets to connect bundle of parallel tubes structure, volume is larger, heat transfer temperature difference is less, easily subregion, tube pitch is larger, and self-constriction ability is poor, generally be applicable to the heat exchange of sub-thread stream, heat exchange efficiency is lower, is difficult to, by natural gas cooling and liquefaction in a flow process, be difficult for three plume uniform heat exchange processes.The present invention has developed and can bear 6.4MPa pressure ,-120 ℃ of low temperature 9Ni steel three plume spiral winding pipe type cryogenic heat exchangers, can complete three plume heat transfer process under high pressure low temperature operating mode; Adopt C 2h 4before cold-producing medium throttling, cross cold technique to produce enough colds, precooling N 2-CH 4mix refrigerant, the cold C of mistake 2h 4cold-producing medium and at LNG secondary refrigerating section liquefied natural gas.
Technical characterstic of the present invention:
The present invention is mainly for the LNG low-temperature liquefaction secondary three plume spiral winding pipe type heat exchange equipments that freeze, employing has that volume is little, heat exchange efficiency is high, heat transfer temperature difference is large, have self-tightening shrinks the three plume spiral winding tube type heat exchangers of adjusting function as main heat exchange equipment, application C 2h 4after the first precooling of cold-producing medium, the refrigeration process flow process of throttling, controls freezing by change of state flow process, and then controls natural gas liquefaction temperature and pressure, improves heat exchange efficiency, solves natural gas-53 ℃～-120 ℃ secondary low-temperature liquefaction problems; Secondary process of refrigerastion has compact conformation with three plume spiral winding tube type heat exchangers, medium band phase-change heat transfer, heat transfer coefficient is large, the precooling of natural gas secondary mix refrigerant, a natural gas in low temperature liquefaction technology difficult problem in Large LNG low-temperature liquefaction process be can solve, system heat exchange and liquefaction efficiency improved; After application secondary LNG low-temperature liquefaction process, 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 installation, once there is the problems such as pipe leakage, be easy to detect, be difficult for causing whole heat exchanger to scrap and the stopping production of set technique equipment; LNG low-temperature liquefaction secondary freezes three plume spiral winding pipe type heat exchange equipments can reasonable distribution liquefaction stages and the thermic load of super cooled sect, make that liquefaction stages is relative with super cooled sect to be coordinated, can be in conjunction with the load distribution of large heat exchanger and heat exchanger tube strength characteristics, the mode of employing sectional center cylinder winding screw coil pipe, guarantees winding process evenly theoretically and intensity meets designing requirement; Choose reasonable the method for heat exchanger inlet and outlet position and material, the multiple tubule plate of employing side can make heat exchanger structure compacter, heat transfer process is optimized; The outer medium counter flow of spiral winding tube type heat exchanger pipe lateral cross are skimmed over winding pipe, and heat exchanger is heat exchanger tube reverse-winding between layers, even if Reynolds number is lower, it is still turbulent flow form, and the coefficient of heat transfer is larger; Owing to being medium band phase-change heat-exchange process, less to the pressure reduction between different medium and temperature difference restriction requirement, process units operation easier reduces, and security is improved; Spiral winding tube type heat exchanger is high pressure resistant and sealing is reliable, thermal expansion can automatic compensating, easily realizes Large LNG liquefaction operation.
Accompanying drawing explanation
Figure 1 shows that LNG low-temperature liquefaction secondary freeze critical piece structure and the position relationship of three plume spiral winding pipe type heat exchange equipments.
The specific embodiment
The natural gas line that by first class outlet temperature is-53 ℃ is connected with Imported gas adapter 29, natural gas-53 ℃, enter Imported gas bobbin carriage 30 during 5.8MPa, reallocate in the each arm of natural gas helical bundle 32 bobbin carriage 30 is interior, tube bank 32 is the C cylindrical shell 12 in and after throttling after spiral winding 2h 4, from three grades and enter and take over 2 N 2-CH 4mix refrigerant carries out heat exchange, and temperature liquefies while being down to-120 ℃, Pressure Drop to 5.5MPa, flow to bobbin carriage 39 after liquefaction, excessively cold by taking over 40 inflow three tier structure device for cooling.
N 2-CH 4mix refrigerant-53 ℃, enter mix refrigerant precooling bobbin carriage 17 during 1.88MPa, reallocate in tube bank 15 each arms bobbin carriage 17 is interior, tube bank 15 is interior by the C after throttling at cylindrical shell 12 after spiral winding 2h 4, from three grades and enter-130 ℃ of shell side, the N of 0.3MPa by taking over 2 2-CH 4mix refrigerant precooling, N in tube side after precooling 2-CH 4cH in mix refrigerant 4be liquefied, form biphase gas and liquid flow, then flow to bobbin carriage 9, temperature is down to-120 ℃, Pressure Drop to 1.58MPa, then sends into the precooling of three tier structure device for cooling through taking over 8.
C 2h 4cold-producing medium-53 ℃, enter bobbin carriage 26 during 1.88MPa, reallocate in C bobbin carriage 26 is interior 2h 4the each arm of supercooling tube bundle 20, tube bank 20 is interior by the C after throttling at cylindrical shell 12 after spiral winding 2h 4, from three grades and enter-130 ℃ of shell side, the N of 0.3MPa by taking over 2 2-CH 4mix refrigerant is excessively cold, crosses after cold and flow to bobbin carriage 5, and temperature is down to-120 ℃, Pressure Drop to 1.58MPa; Cross the C after cold 2h 4through take over 4 and take over the choke valve throttling between 43 after Pressure Drop to 0.3MPa, temperature becomes-119.4 ℃, in supercooled liquid phase state; C after throttling 2h 4through taking over 43, enter cylindrical shell 12, with the N from taking over 2 2-CH 4mix refrigerant flows downward after mixing, cooling N 2-CH 4tube bank, C 2h 4after tube bank and natural gas tube bank ,-63 ℃, during 0.3MPa through taking over three grades of heat exchangers of 21 outflow, enter LNG one-level heat exchange equipment.

Claims (1)

  1. The 1.LNG low-temperature liquefaction secondary three plume spiral winding pipe type heat exchange equipments that freeze, comprise N 2-CH 4Shell side suction flange (1), N 2-CH 4Shell side entrance sleeve (2), C 2H 4Outlet(discharge) flange (3), C 2H 4Discharge connection (4), C 2H 4Outlet bobbin carriage (5), C 2H 4Outlet tube sheet (6), N 2-CH 4Outlet(discharge) flange (7), N 2-CH 4Discharge connection (8), N 2-CH 4Outlet bobbin carriage (9), N 2-CH 4Outlet tube sheet (10), N 2-CH 4Outlet tube bank (11), cylindrical shell (12), spiral coil (13), lower support circle (14), N 2-CH 4Import tube bank (15), N 2-CH 4Import tube sheet (16), N 2-CH 4Import bobbin carriage (17), N 2-CH 4Suction flange (18), N 2-CH 4Entrance sleeve (19), C 2H 4Import tube bank (20), C 2H 4-N 2-CH 4Mixed gas outlet is taken over (21), C 2H 4-N 2-CH 4Mixed gas outlet flange (22), low head (23), C 2H 4Suction flange (24), C 2H 4Entrance sleeve (25), C 2H 4Import bobbin carriage (26), C 2H 4Import tube sheet (27), Imported gas flange (28), Imported gas are taken over (29), Imported gas bobbin carriage (30), Imported gas tube sheet (31), Imported gas tube bank (32), central tube (33), filler strip (34), ear seat (35), upper bracing ring (36), C 2H 4C after precooling outlet tube bank (37), gas outlet tube bank (38), gas outlet bobbin carriage (39), gas outlet adapter (40), gas outlet flange (41), gas outlet tube sheet (42), throttling 2H 4C after entrance sleeve (43), throttling 2H 4Suction flange (44),Upper cover (45), is characterized in that: Imported gas tube bank (32), N 2-CH 4Import tube bank (15), C 2H 4Import tube bank (20) is wound around around central tube (33), and the tube core after winding is installed in cylindrical shell (12); Bracing ring (36) is installed in central tube (33) one end, and lower support circle (14) is installed in one end, and upper bracing ring (36) is fixed on cylindrical shell (12) top, and lower support circle (14) is fixed on cylindrical shell (12) bottom, Imported gas tube bank (32), N 2-CH 4Import tube bank (15), C 2H 4Import tube bank (20) is wound between bracing ring (36) and lower support circle (14); Cylindrical shell (12) top is connected with upper cover (45), and N is installed at upper cover (45) top 2-CH 4Shell side entrance sleeve (2) and N 2-CH 4Shell side suction flange (1); Cylindrical shell (12) bottom is connected with low head (23), and C is installed at low head (23) top 2H 4-N 2-CH 4Mixed gas outlet is taken over (21) and C 2H 4-N 2-CH 4Mixed gas outlet flange (22); Cylindrical shell (12) upper left-hand is installed N 2-CH 4Outlet tube sheet (10), N 2-CH 4Outlet tube sheet (10) right side connects N 2-CH 4Outlet tube bank (11), left side connects N 2-CH 4Outlet bobbin carriage (9), N 2-CH 4Outlet bobbin carriage (9) top connects N 2-CH 4Discharge connection (8) and N 2-CH 4Outlet(discharge) flange (7); Cylindrical shell (12) upper right is installed gas outlet tube sheet (42), gas outlet tube sheet (42) left side connects gas outlet tube bank (38), right side connects gas outlet bobbin carriage (39), and gas outlet bobbin carriage (39) top connects gas outlet and takes over (40) and gas outlet flange (41); In the middle of cylindrical shell (12) top, C is installed in below 2H 4Outlet tube sheet (6), C 2H 4Outlet tube sheet (6) is installed C above 2H 4Precooling outlet tube bank (37), after C is installed 2H 4Outlet bobbin carriage (5), C 2H 4C is installed at outlet bobbin carriage (5) top 2H 4Discharge connection (4) and C 2H 4Outlet(discharge) flange (3); C after the middle upper part installation throttling of cylindrical shell (12) top 2H 4Entrance sleeve (43),C after throttling 2H 4Suction flange (44); Cylindrical shell (12) lower left side is installed N 2-CH 4Import tube sheet (16), N 2-CH 4Import tube sheet (16) right side connects N 2-CH 4Import tube bank (15) import, left side connects N 2-CH 4Import bobbin carriage (17), N 2-CH 4N is installed at import bobbin carriage (17) top 2-CH 4Entrance sleeve (19) and N 2-CH 4Suction flange (18); Imported gas tube sheet (31) is installed on cylindrical shell (12) right side, bottom, Imported gas tube sheet (31) left side connects Imported gas tube bank (32) import, right side connects Imported gas bobbin carriage (30), and Imported gas bobbin carriage (30) top is installed Imported gas and taken over (29) and Imported gas flange (28); C is installed in the middle of cylindrical shell (12) bottom 2H 4Import tube sheet (27), C 2H 4Import tube sheet (27) is installed C above 2H 4Import tube bank (20), after C is installed 2H 4Import bobbin carriage (26), C 2H 4C is installed at import bobbin carriage (26) top 2H 4Entrance sleeve (25) and C 2H 4Suction flange (24); Cylindrical shell (12) middle part mounting ear seat (35).
CN201110376419.3A 2011-11-24 2011-11-24 Three-stream spiral wound type heat exchange equipment for secondary refrigeration and low-temperature liquefaction of LNG (liquefied natural gas) Expired - Fee Related CN102538388B (en)

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