CN102538388A - 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 PDFInfo
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- CN102538388A CN102538388A CN2011103764193A CN201110376419A CN102538388A CN 102538388 A CN102538388 A CN 102538388A CN 2011103764193 A CN2011103764193 A CN 2011103764193A CN 201110376419 A CN201110376419 A CN 201110376419A CN 102538388 A CN102538388 A CN 102538388A
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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
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, use C
2H
4Cold-producing medium and LNG secondary import 0.3MPa ,-130 ℃ N
2-CH
4Mixed refrigerant vapor is cooled to-120 ℃ and liquefaction with 5.8MPa ,-53 ℃ of natural gases in three plume spiral winding pipe formula heat exchangers, so that LNG gets into three grades of super cooled sects; The secondary three plume spiral winding pipe formula heat exchangers that freeze are at first crossed cold C
2H
4Cold-producing medium, C
2H
4Cross and be throttled into shell side and N after cold
2-CH
4Mix-53 ℃ LNG tube banks, the N of back cooling from one-level
2-CH
4Precooling tube bank and C
2H
4The supercooling tube bundle makes natural gas and N in the tube side
2-CH
4Middle CH
4Liquefaction reached cold C
2H
4, precooling N
2-CH
4And liquefied natural gas purpose; 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 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 secondary low-temperature 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 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 core technology problem, i.e. LNG low-temperature liquefaction secondary three plume spiral winding pipe formula heat exchanger structure and the technological process problems of freezing.
Summary of the invention
The present invention is primarily aimed at 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 big, have three plume spiral winding pipe formula heat exchangers that self-tightening shrinks the adjustment function as main heat exchange equipment, application C
2H
4The refrigeration process flow process of throttling after the precooling of cold-producing medium 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 secondary low-temperature liquefaction problem.
Technical solution of the present invention:
Freeze three plume spiral winding pipe formula heat exchange equipment of LNG low-temperature liquefaction secondary comprises 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
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, following bracing ring 14, N
2-CH
4Import 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
4Import 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, natural gas suction flange 28, natural gas entrance sleeve 29, natural gas import bobbin carriage 30, natural gas import tube sheet 31, natural gas import tube bank 32, central tube 33, filler strip 34, ear seat 35, last 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, the throttling
2H
4C after entrance sleeve 43, the throttling
2H
4Suction flange 44, upper cover 45 is characterized in that: natural gas helical bundle 32, N
2-CH
4 Helical bundle 15, C
2H
4Helical bundle 20 twines around central tube 33, and the tube core after the winding is installed in the cylindrical shell 12; Central tube 33 1 ends are installed bracing ring 36, one ends bracing ring 14 down are installed, and last bracing ring 36 is fixed in cylindrical shell 12 tops, and following bracing ring 14 is fixed in cylindrical shell 12 bottoms, natural gas helical bundle 32, N
2-CH
4 Helical bundle 15, C
2H
4Helical bundle 20 is wound between bracing ring 36 and the following bracing ring 14; Cylindrical shell 12 tops are connected with end socket 45, and adapter 2 and flange 1 are installed in end socket 45 tops; Cylindrical shell 12 bottoms are connected with end socket 23, and adapter 21 and flange 22 are installed in end socket 23 tops; Cylindrical shell 12 upper left-hand are installed N
2-CH
4Refrigerant outlet tube sheet 10, tube sheet 10 right sides connect N
2-CH
4Mix refrigerant outlet tube bank 11, the left side connects bobbin carriage 9, and bobbin carriage 9 tops connect adapter 8 and flange 7; Cylindrical shell 12 upper right installation gas outlet tube sheet 42, tube sheet 42 left sides connect gas outlet tube bank 38, and the right side connects bobbin carriage 39, and bobbin carriage 39 tops connect adapter 40 and flange 41; C is installed in the below in the middle of cylindrical shell 12 tops
2H
4 Outlet tube sheet 6, C is installed in tube sheet 6 fronts
2H
4Precooling outlet tube bank 37, C is installed in the back
2H
4Outlet bobbin carriage 5, adapter 4 and flange 3 are installed in outlet bobbin carriage 5 tops; C after the cylindrical shell 12 top middle upper parts installation throttlings
2H
4C after entrance sleeve 43, the throttling
2H
4Suction flange 44; Cylindrical shell 12 lower left side are installed N
2-CH
4 Import tube sheet 16, tube sheet 16 right sides connect N
2-CH
415 imports are restrained in precooling, and the left side connects N
2-CH
4Import bobbin carriage 17, adapter 19 and flange 18 are installed in bobbin carriage 17 tops; Natural gas import tube sheet 31 is installed on right side, cylindrical shell 12 bottom, and tube sheet 31 left sides connect the natural gas precooling and restrain 32 imports, and the right side connects natural gas import bobbin carriage 30, and adapter 29 and flange 28 are installed in bobbin carriage 30 tops; C is installed in the middle of cylindrical shell 12 bottoms
2H
4 Import tube sheet 27, C is installed in tube sheet 27 fronts
2H
4Precooling import tube bank 20, C is installed in the back
2H
4Outlet bobbin carriage 26, adapter 25 and flange 24 are installed in outlet bobbin carriage 26 tops; Cylindrical shell 12 middle part mounting ear seats 35.
C
2H
4Cold-producing medium-53 ℃, get into bobbin carriage 26 during 1.88MPa, in bobbin carriage 26, be allocated in C
2H
4Supercooling tube bundle 20 each arm, tube bank 20 after spiral twines in cylindrical shell 12 by the C after the throttling
2H
4, take over 2 certainly and get into-130 ℃ of housings, the N of 0.3MPa
2-CH
4Mix refrigerant is cold excessively; Temperature is reduced to-120 ℃, pressure and is reduced to 1.58MPa; Flowing to bobbin carriage 5 again, is subcooled liquid through the choke valve throttling that is installed on adapter 4 and take between 43, and pressure is reduced to 0.3MPa after the throttling; Temperature becomes-119.4 ℃, again through take over 43 get into cylindrical shells 12 with from three grades take over certainly 2 get into housings N
2-CH
4Mist mixes, the cooled natural gas that flows downward after mixing tube bank 32, N
2-CH
4Precooling tube bank 15, C
2H
4Behind the supercooling tube bundle 20 ,-63 ℃, flow out the two-stage system device for cooling and get into the one-level refrigerating section through taking over 21 during 0.3MPa.
N
2-CH
4Mist-53 ℃, get into N during 1.88MPa
2-CH
4Precooling bobbin carriage 17 is allocated in precooling tube bank 15 each arm in bobbin carriage 17, tube bank 15 after spiral twines in cylindrical shell 12 by the C after the throttling
2H
4, certainly take over 2 get into housings N
2-CH
4The mix refrigerant precooling, CH after the precooling
4Be liquefied and form N
2-CH
4Biphase gas and liquid flow, temperature are reduced to-120 ℃, pressure and are reduced to 1.58MPa, flow to bobbin carriage 9 again, through taking over 8 back entering three tier structure device for cooling precoolings.
Natural gas-53 ℃, get into natural gas import bobbin carriage 30 during 5.8MPa, in bobbin carriage 30, be allocated in natural gas helical bundle 32 each arm, tube bank 32 is twined the back in cylindrical shell 12 and the C after the throttling through spiral
2H
4, certainly take over 2 get into housings N
2-CH
4Mix refrigerant carries out heat exchange, and temperature is reduced to-120 ℃, liquefied when pressure is reduced to 5.5MPa, flow to bobbin carriage 39 after the liquefaction, flows out the two-stage system device for cooling and gets into three grades of super cooled sects through taking over 40 again.
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 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
4The cold-producing medium refrigeration process solves second section low-temperature liquefaction process equipment problem.Research process is relatively independent, can be connected to become integral body for two sections with front and back, and 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 install.Secondly, adopt C
2H
4Behind the cold-producing medium refrigeration process, must be before the throttling to C
2H
4Carried out cold.The cryogen import is 1.88MPa ,-53 ℃ the time, C
2H
4Be in liquid phase state, when pressure reach 1.58MPa, when temperature reaches-120 ℃, C
2H
4Cross cold and have big sensible heat, can obtain bigger refrigerating capacity after the throttling again.N
2-CH
4Mix refrigerant is mainly used in the cold process of three tier structure, must be before the throttling through-53 ℃～-120 ℃ ,-120 ℃～-164 ℃ two sections low temperature precooling process, and in the 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 adopted two large tubesheets to connect the bundle of parallel tubes structure, and volume is bigger, and heat transfer temperature difference is less; Be prone to subregion, tube pitch is bigger, and the self-constriction ability is relatively poor; Generally be applicable to 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 the three plume uniform heat exchange processes of accomplishing.The present invention has developed and can bear 6.4MPa pressure ,-120 ℃ of low temperature 9Ni steel three plume spiral winding pipe formula cryogenic heat exchangers, can accomplish three plume heat transfer process under the high pressure low temperature operating mode; Adopt C
2H
4Cross cold technology before the cold-producing medium throttling to produce enough colds, precooling N
2-CH
4Mix refrigerant, the cold C of mistake
2H
4Cold-producing medium reaches at LNG secondary refrigerating section liquefied natural gas.
Technical characterstic of the present invention:
The present invention is primarily aimed at freeze three plume spiral winding pipe formula heat exchange equipment of LNG low-temperature liquefaction secondary; Employing has that volume is little, heat exchange efficiency is high, heat transfer temperature difference is big, have three plume spiral winding pipe formula heat exchangers that self-tightening shrinks adjustment function as main heat exchange equipment, application C
2H
4The refrigeration process flow process of throttling after the precooling of cold-producing medium 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-53 ℃～-120 ℃ secondary low-temperature liquefaction problems; The secondary process of refrigerastion has compact conformation with three plume spiral winding pipe formula heat exchangers; Multiple medium band phase-change heat transfer; Heat transfer coefficient is big; The precooling of natural gas secondary mix refrigerant, a natural gas in low temperature liquefaction technology difficult problem in the Large LNG low-temperature liquefaction process be can solve, system's heat exchange and liquefaction efficiency improved; After using secondary LNG low-temperature liquefaction process, 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; The thermic load of three plume spiral winding pipe formula heat exchange equipment reasonable distribution liquefaction stages and super cooled sect but LNG low-temperature liquefaction secondary freezes; Liquefaction stages and super cooled sect are coordinated relatively; The load distribution and the heat exchanger tube strength characteristics that can combine large 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 1ly be LNG low-temperature liquefaction secondary freeze the critical piece structure and the position relation of three plume spiral winding pipe formula heat exchange equipments.
The specific embodiment
The natural gas line that with first class outlet temperature is-53 ℃ is connected with natural gas entrance sleeve 29; Natural gas-53 ℃, get into natural gas import bobbin carriage 30 during 5.8MPa; In bobbin carriage 30, reallocate in natural gas helical bundle 32 each arm, tube bank 32 is twined the back in cylindrical shell 12 and the C after the throttling through spiral
2H
4, from three grades and get into to take over 2 N
2-CH
4Mix refrigerant carries out heat exchange, and temperature is reduced to-120 ℃, liquefied when pressure is reduced to 5.5MPa, flow to bobbin carriage 39 after the liquefaction, and is cold excessively through taking over 40 inflow three tier structure device for cooling.
N
2-CH
4Mix refrigerant-53 ℃, get into mix refrigerant precooling bobbin carriage 17 during 1.88MPa, in bobbin carriage 17, reallocate in tube bank 15 each arm, tube bank 15 after spiral twines in cylindrical shell 12 by the C after the throttling
2H
4, from three grades and get into-130 ℃ of shell sides, the N of 0.3MPa by taking over 2
2-CH
4The mix refrigerant precooling, N in the tube side after the precooling
2-CH
4CH in the mix refrigerant
4Be liquefied, form biphase gas and liquid flow, flow to bobbin carriage 9 again, temperature is reduced to-120 ℃, pressure and is reduced to 1.58MPa, sends into the precooling of three tier structure device for cooling through taking over 8 again.
C
2H
4Cold-producing medium-53 ℃, get into bobbin carriage 26 during 1.88MPa, in bobbin carriage 26, reallocate in C
2H
4Supercooling tube bundle 20 each arm, tube bank 20 after spiral twines in cylindrical shell 12 by the C after the throttling
2H
4, from three grades and get into-130 ℃ of shell sides, the N of 0.3MPa by taking over 2
2-CH
4Mix refrigerant is cold excessively, crosses to flow to bobbin carriage 5 after cold, and temperature is reduced to-120 ℃, pressure and reduced to 1.58MPa; Cross the C after cold
2H
4Pressure is reduced to 0.3MPa after the choke valve throttling between adapter 4 and the adapter 43, and temperature becomes-119.4 ℃, is in supercooled liquid phase state; C after the throttling
2H
4Get into cylindrical shell 12 through taking over 43, with N from adapter 2
2-CH
4Mix refrigerant flows downward after mixing, cooling N
2-CH
4Tube bank, C
2H
4After tube bank and the natural gas tube bank ,-63 ℃, flow out three grades of heat exchangers through taking over 21 during 0.3MPa, get into LNG one-level heat exchange equipment.
Claims (4)
- Three plume spiral winding pipe formula heat exchange equipment comprises N 1.LNG the low-temperature liquefaction secondary freezes 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, following bracing ring 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 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 4Import bobbin carriage 26, C 2H 4Import tube sheet 27, natural gas suction flange 28, natural gas entrance sleeve 29, natural gas import bobbin carriage 30, natural gas import tube sheet 31, natural gas import tube bank 32, central tube 33, filler strip 34, ear seat 35, last 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, the throttling 2H 4C after entrance sleeve 43, the throttling 2H 4Suction flange 44, upper cover 45 is characterized in that: natural gas helical bundle 32, N 2-CH 4Helical bundle 15, C 2H 4Helical bundle 20 twines around central tube 33, and the tube core after the winding is installed in the cylindrical shell 12; Central tube 33 1 ends are installed bracing ring 36, one ends bracing ring 14 down are installed, and last bracing ring 36 is fixed in cylindrical shell 12 tops, and following bracing ring 14 is fixed in cylindrical shell 12 bottoms, natural gas helical bundle 32, N 2-CH 4Helical bundle 15, C 2H 4Helical bundle 20 is wound between bracing ring 36 and the following bracing ring 14; Cylindrical shell 12 tops are connected with end socket 45, and adapter 2 and flange 1 are installed in end socket 45 tops; Cylindrical shell 12 bottoms are connected with end socket 23, and adapter 21 and flange 22 are installed in end socket 23 tops; Cylindrical shell 12 upper left-hand are installed N 2-CH 4Refrigerant outlet tube sheet 10, tube sheet 10 right sides connect N 2-CH 4Mix refrigerant outlet tube bank 11, the left side connects bobbin carriage 9, and bobbin carriage 9 tops connect adapter 8 and flange 7; Cylindrical shell 12 upper right installation gas outlet tube sheet 42, tube sheet 42 left sides connect gas outlet tube bank 38, and the right side connects bobbin carriage 39, and bobbin carriage 39 tops connect adapter 40 and flange 41; C is installed in the below in the middle of cylindrical shell 12 tops 2H 4Outlet tube sheet 6, C is installed in tube sheet 6 fronts 2H 4Precooling outlet tube bank 37, C is installed in the back 2H 4Outlet bobbin carriage 5, adapter 4 and flange 3 are installed in outlet bobbin carriage 5 tops; C after the cylindrical shell 12 top middle upper parts installation throttlings 2H 4C after entrance sleeve 43, the throttling 2H 4Suction flange 44; Cylindrical shell 12 lower left side are installed N 2-CH 4Import tube sheet 16, tube sheet 16 right sides connect N 2-CH 415 imports are restrained in precooling, and the left side connects N 2-CH 4Import bobbin carriage 17, adapter 19 and flange 18 are installed in bobbin carriage 17 tops; Natural gas import tube sheet 31 is installed on right side, cylindrical shell 12 bottom, and tube sheet 31 left sides connect the natural gas precooling and restrain 32 imports, and the right side connects natural gas import bobbin carriage 30, and adapter 29 and flange 28 are installed in bobbin carriage 30 tops; C is installed in the middle of cylindrical shell 12 bottoms 2H 4Import tube sheet 27, C is installed in tube sheet 27 fronts 2H 4Precooling import tube bank 20, C is installed in the back 2H 4Outlet bobbin carriage 26, adapter 25 and flange 24 are installed in outlet bobbin carriage 26 tops; Cylindrical shell 12 middle part mounting ear seats 35.
- 2. according to claim 1Freeze three plume spiral winding pipe formula heat exchange equipment of described LNG low-temperature liquefaction secondary is characterized in that: C 2H 4Cold-producing medium-53 ℃, get into bobbin carriage 26 during 1.88MPa, in bobbin carriage 26, be allocated in C 2H 4Supercooling tube bundle 20 each arm, tube bank 20 after spiral twines in cylindrical shell 12 by the C after the throttling 2H 4, take over 2 certainly and get into-130 ℃ of housings, the N of 0.3MPa 2-CH 4Mix refrigerant is cold excessively; Temperature is reduced to-120 ℃, pressure and is reduced to 1.58MPa; Flowing to bobbin carriage 5 again, is subcooled liquid through the choke valve throttling that is installed on adapter 4 and take between 43, and pressure is reduced to 0.3MPa after the throttling; Temperature becomes-119.4 ℃, again through take over 43 get into cylindrical shells 12 with from three grades take over certainly 2 get into housings N 2-CH 4Mist mixes, the cooled natural gas that flows downward after mixing tube bank 32, N 2-CH 4Precooling tube bank 15, C 2H 4Behind the supercooling tube bundle 20 ,-63 ℃, flow out the two-stage system device for cooling and get into the one-level refrigerating section through taking over 21 during 0.3MPa.
- 3. according to claim 1Described LNG low-temperature liquefaction secondary refrigeration spiral winding pipe formula heat exchange equipment is characterized in that: N 2-CH 4Mist-53 ℃, get into N during 1.88MPa 2-CH 4Precooling bobbin carriage 17 is allocated in precooling tube bank 15 each arm in bobbin carriage 17, tube bank 15 after spiral twines in cylindrical shell 12 by the C after the throttling 2H 4, certainly take over 2 get into housings N 2-CH 4The mix refrigerant precooling, CH after the precooling 4Be liquefied and form N 2-CH 4Biphase gas and liquid flow, temperature are reduced to-120 ℃, pressure and are reduced to 1.58MPa, flow to bobbin carriage 9 again, through taking over 8 back entering three tier structure device for cooling precoolings.
- 4. according to claim 1Freeze three plume spiral winding pipe formula heat exchange equipment of described LNG low-temperature liquefaction secondary; It is characterized in that: natural gas-53 ℃, get into natural gas import bobbin carriage 30 during 5.8MPa; In bobbin carriage 30, be allocated in natural gas helical bundle 32 each arm, tube bank 32 is twined the back in cylindrical shell 12 and the C after the throttling through spiral 2H 4, certainly take over 2 get into housings N 2-CH 4Mix refrigerant carries out heat exchange, and temperature is reduced to-120 ℃, liquefied when pressure is reduced to 5.5MPa, flow to bobbin carriage 39 after the liquefaction, flows out the two-stage system device for cooling and gets into three grades of super cooled sects through taking over 40 again.
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|---|---|---|---|
| CN201110376419.3A CN102538388B (en) | 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) |
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|---|---|---|---|
| CN201110376419.3A CN102538388B (en) | 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) |
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| CN102538388A true CN102538388A (en) | 2012-07-04 |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103438736A (en) * | 2013-08-19 | 2013-12-11 | 张周卫 | Two-stage back heating multi-strand winding pipe type heat exchange device for low-temperature liquid nitrogen |
| CN103438733A (en) * | 2013-08-31 | 2013-12-11 | 张周卫 | Primary heat-regeneration multi-flow heat exchange device for low-temperature liquid nitrogen |
| CN103542742A (en) * | 2013-11-02 | 2014-01-29 | 福州大学 | Core-pulling heat exchanger |
| CN106931805A (en) * | 2017-04-12 | 2017-07-07 | 中国石油大学(华东) | A kind of new bifilar stream wrap-round tubular heat exchanger |
| CN112082410A (en) * | 2020-09-22 | 2020-12-15 | 山东省城乡规划设计研究院 | Spray type shell-and-tube heat exchanger arranged in staggered manner from top to bottom |
| CN112113442A (en) * | 2020-09-22 | 2020-12-22 | 山东省城乡规划设计研究院 | Jet shell-and-tube heat exchanger with staggered upper and lower intervals |
| CN114152117A (en) * | 2021-12-02 | 2022-03-08 | 中国石油大学(华东) | LNG is around tubular heat exchanger |
| CN115289872A (en) * | 2022-09-28 | 2022-11-04 | 安徽普泛能源技术有限公司 | Quaternary efficient heat exchanger and absorption type ice making system and application thereof |
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Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103438736A (en) * | 2013-08-19 | 2013-12-11 | 张周卫 | Two-stage back heating multi-strand winding pipe type heat exchange device for low-temperature liquid nitrogen |
| CN103438736B (en) * | 2013-08-19 | 2015-05-27 | 张周卫 | Two-stage back heating multi-strand winding pipe type heat exchange device for low-temperature liquid nitrogen |
| CN103438733A (en) * | 2013-08-31 | 2013-12-11 | 张周卫 | Primary heat-regeneration multi-flow heat exchange device for low-temperature liquid nitrogen |
| CN103438733B (en) * | 2013-08-31 | 2015-07-01 | 张周卫 | Primary heat-regeneration multi-flow heat exchange device for low-temperature liquid nitrogen |
| CN103542742A (en) * | 2013-11-02 | 2014-01-29 | 福州大学 | Core-pulling heat exchanger |
| CN103542742B (en) * | 2013-11-02 | 2015-09-09 | 福州大学 | Can to loose core heat exchanger |
| CN106931805A (en) * | 2017-04-12 | 2017-07-07 | 中国石油大学(华东) | A kind of new bifilar stream wrap-round tubular heat exchanger |
| CN112082410A (en) * | 2020-09-22 | 2020-12-15 | 山东省城乡规划设计研究院 | Spray type shell-and-tube heat exchanger arranged in staggered manner from top to bottom |
| CN112113442A (en) * | 2020-09-22 | 2020-12-22 | 山东省城乡规划设计研究院 | Jet shell-and-tube heat exchanger with staggered upper and lower intervals |
| CN114152117A (en) * | 2021-12-02 | 2022-03-08 | 中国石油大学(华东) | LNG is around tubular heat exchanger |
| CN114152117B (en) * | 2021-12-02 | 2024-03-19 | 中国石油大学(华东) | LNG winds tubular heat exchanger |
| CN115289872A (en) * | 2022-09-28 | 2022-11-04 | 安徽普泛能源技术有限公司 | Quaternary efficient heat exchanger and absorption type ice making system and application thereof |
| CN115289872B (en) * | 2022-09-28 | 2023-02-07 | 安徽普泛能源技术有限公司 | Quaternary efficient heat exchanger and absorption type ice making system and application thereof |
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