CN115046326A - Binary refrigeration start system and method for light hydrocarbon cracking device - Google Patents
Binary refrigeration start system and method for light hydrocarbon cracking device Download PDFInfo
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- CN115046326A CN115046326A CN202210612493.9A CN202210612493A CN115046326A CN 115046326 A CN115046326 A CN 115046326A CN 202210612493 A CN202210612493 A CN 202210612493A CN 115046326 A CN115046326 A CN 115046326A
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- 238000005057 refrigeration Methods 0.000 title claims abstract description 59
- 238000000034 method Methods 0.000 title claims abstract description 36
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 29
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 29
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 29
- 238000005336 cracking Methods 0.000 title claims abstract description 28
- 239000000463 material Substances 0.000 claims abstract description 126
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 96
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 59
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 29
- 239000003507 refrigerant Substances 0.000 claims description 66
- 239000007789 gas Substances 0.000 claims description 42
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 17
- 239000005977 Ethylene Substances 0.000 claims description 17
- 239000012071 phase Substances 0.000 claims description 12
- 238000012360 testing method Methods 0.000 claims description 12
- 230000008569 process Effects 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 9
- 230000008859 change Effects 0.000 claims description 8
- 238000006073 displacement reaction Methods 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 7
- 239000003345 natural gas Substances 0.000 claims description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 239000007791 liquid phase Substances 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 5
- 238000001179 sorption measurement Methods 0.000 claims description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims description 4
- 238000011144 upstream manufacturing Methods 0.000 claims description 4
- 230000001502 supplementing effect Effects 0.000 claims description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 2
- 239000001569 carbon dioxide Substances 0.000 claims description 2
- 238000010926 purge Methods 0.000 claims description 2
- 230000005540 biological transmission Effects 0.000 claims 2
- 238000012824 chemical production Methods 0.000 abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 230000001276 controlling effect Effects 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 5
- 230000009467 reduction Effects 0.000 description 5
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 4
- 239000002808 molecular sieve Substances 0.000 description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 238000010276 construction Methods 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 238000011835 investigation Methods 0.000 description 3
- 238000005192 partition Methods 0.000 description 3
- 238000003825 pressing Methods 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000007689 inspection Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 230000003321 amplification Effects 0.000 description 1
- 229910002056 binary alloy Inorganic materials 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- -1 propylene, ethylene, methane Chemical class 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000012549 training Methods 0.000 description 1
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B9/00—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point
- F25B9/002—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant
- F25B9/006—Compression machines, plants or systems, in which the refrigerant is air or other gas of low boiling point characterised by the refrigerant the refrigerant containing more than one component
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
- C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
- C07C4/06—Catalytic processes
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B41/00—Fluid-circulation arrangements
- F25B41/20—Disposition of valves, e.g. of on-off valves or flow control valves
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B43/00—Arrangements for separating or purifying gases or liquids; Arrangements for vaporising the residuum of liquid refrigerant, e.g. by heat
- F25B43/006—Accumulators
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B49/00—Arrangement or mounting of control or safety devices
- F25B49/02—Arrangement or mounting of control or safety devices for compression type machines, plants or systems
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- General Engineering & Computer Science (AREA)
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- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
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Abstract
The invention discloses a binary refrigeration start system and a binary refrigeration start method for a light hydrocarbon cracking device, which belong to the technical field of chemical production, and comprise a tank car and a heat exchanger, wherein material flows are filled in the tank car, the tank car is communicated with the heat exchanger through a pipeline, and a valve a, an 8-shaped blind plate a, a blind cover pilot shower valve a and a valve b are sequentially arranged on the connected pipeline; the heat exchanger is communicated with the suction tank through a pipeline, and a pressure gauge a, a one-way check valve a, a blind cover pilot shower valve b, an 8-shaped blind plate b and a valve c are sequentially arranged on the connected pipeline; the medium-pressure nitrogen is communicated with the heat exchanger through a pipeline, and a valve d, a pilot shower valve a with a pipe cap, a one-way check valve b, a pressure gauge b and a thermometer a are sequentially arranged on the connected pipeline; the heat exchanger is communicated with a low-pressure nitrogen pipe network through a pipeline, and a valve h, a one-way check valve c, a pipe cap-equipped guide shower b, an 8-shaped blind plate c, a valve h and a pressure gauge d are sequentially arranged on the connected pipeline. The technical problem of low driving speed caused by impure methane during initial driving of the equipment is solved, and the method is mainly applied to the aspect of chemical production.
Description
Technical Field
The invention belongs to the technical field of chemical production, and particularly relates to a binary refrigeration system and a binary refrigeration method for driving a light hydrocarbon cracking device.
Background
Along with the advocated national energy conservation, consumption reduction, environmental protection and low carbon, the ethylene preparation route by light hydrocarbon cracking has gained more and more attention from industry professional field due to the obvious advantages of high yield, short flow, low energy consumption and the like, but the light hydrocarbon cracking device is often highly integrated with a matched deep cooling unit due to high energy utilization degree and large ethylene separation processing capacity, and needs to adopt refrigerants such as propylene, ethylene, methane and the like for refrigeration, at present, the energy consumption of ternary refrigeration is higher than that of cascade refrigeration, the energy consumption of binary refrigeration is lower than that of cascade refrigeration, and the binary refrigeration process is a hot door currently applied.
Binary refrigerants and various material flows at the separation process side are integrated in a large-sized cold box and mutually affect, local disturbance amplification into regional disturbance is easy to occur, and refrigerants with different temperature grades can separate materials with different volatility. Charles in application No. CN200880130589.x describes in more detail the distribution of the binary refrigerant stream in the cold box in the ethylene plant and the interdependence of the methane separation system and the binary refrigerant, and girisy in application No. CN201780086725.9 discloses a binary refrigerant containing methane and ethylene for the demethanization system refrigeration of the ethylene plant, reducing the total energy consumption by installing interstage coolers, but none describes the orchestration of the introduction of the original drive material of the binary refrigeration system. Chendelh light published article "ethylene plant cryogenic system start-up scheme research" in the chemical industry progress disclosure, which indicates that Yanshan petrochemical is the first practice unit for applying binary refrigeration to ethylene plants worldwide, and the schemes provided by the patent packet suppliers are often not satisfactory for guiding the actual start-up process. In the Linpeng, China and foreign energy publicity published 'experience and optimization operation of driving of binary refrigeration system', the problems of unit vibration, anti-surge regulation, liquid level linkage and the like of the driving difficulty of the binary system of Zhongsha (Tianjin) petrochemical are deeply explained.
Ethylene of a binary refrigeration system is generally defined as a material flow led out from a reflux tank at the top of an ethylene rectifying tower in the device, methane is generally from a material flow led out from a reflux tank of a demethanizer, the loss of a supplementary refrigerant in the closed refrigeration cycle process is unanimous, but the technical problems that methane is not introduced in the original starting period, the methane content in the ethylene refrigeration working condition does not reach the design value because of the refrigerant composition, the tail end pressure of a refrigeration unit cannot reach the design value, the refrigeration temperature cannot reach the corresponding grade, the cryogenic methane separation purity is unqualified, the methane cannot be supplemented, a stable demethanizer system is gradually built in tens of days according to the traditional starting method, or unqualified methane (containing ethane) is supplemented into the binary refrigeration system, and the qualified methane is collected and discharged from the bottom of a refrigerant collecting tank, because the boiling points of ethane and ethylene are similar, the purity of the polluted binary refrigerant is difficult to improve after the ethane component is mixed, the pure binary refrigerants (methane and ethylene) are supplemented and replaced to continuously cause energy and material loss, the hydrogen-rich gas discharged from the top of the demethanizer is used for dryer regeneration, the feed water content of the original initial dryer for start-up is usually higher, the adsorption period of the dryer is possible to be less than 48 hours, the carbon two components in the regenerated gas can be coked in a molecular sieve to influence long-period operation, and a large amount of material replacement can be caused during nitrogen regeneration to exhaust a torch.
The technical problems are not described in public periodicals and patents at present, the invention carries out creative practice on the problems, is successful, effectively shortens the period from the initial proportion of the original start-up refrigerant of the binary refrigeration system to the design proportion, ensures the purity of the binary refrigerant, accelerates the progress of the qualified demethanizer effluent, fills the blank of the start-up method of the binary refrigeration system for preparing ethylene by cracking light hydrocarbon in China, and is suitable for being popularized in ethylene plants with the binary refrigeration system.
Disclosure of Invention
In order to solve the technical problems in the background art, the invention provides a binary refrigeration start-up system of a light hydrocarbon cracking device, which adopts the following technical scheme:
a binary refrigeration starting system of a light hydrocarbon cracking device comprises a binary refrigeration system, wherein the binary refrigeration system comprises a refrigerant suction tank, a compressor and a user heat exchanger, the refrigerant suction tank is connected with the user heat exchanger through a pipeline, a first safety valve group is arranged at a refrigerant outlet of the user heat exchanger and comprises a first valve, a second valve, a third valve and a safety valve b, the first safety valve group is connected to a flare gas pipe network through a pipeline, one end of the compressor is connected with the refrigerant suction tank through a pipeline, the other end of the compressor is communicated with a refrigerant collecting tank through a pipeline, a liquid level meter a is arranged on the refrigerant collecting tank, a second safety valve group, a cooling heat exchanger and a thermometer are sequentially arranged on the connected pipeline, the second safety valve group comprises a fourth valve, a regulating valve, a fifth valve and a safety valve c, the second safety valve group enters a flare gas pipe network through a pipeline, and is characterized in that a logistics system c is arranged on the refrigerant suction tank, the logistics system c comprises a tank car and a heat exchanger, the tank car is internally provided with a logistics c, the tank car and the heat exchanger are communicated through a pipeline, and a valve a, an 8-shaped blind plate a, a blind cover pilot valve a and a valve b are sequentially arranged on the connecting pipeline;
the heat exchanger is communicated with a refrigerant suction tank through a pipeline, and a pressure gauge a, a one-way check valve a, a blind cover pilot shower valve b, an 8-shaped blind plate b and a valve c are sequentially arranged on the connected pipeline; the heat exchanger is communicated with a low-pressure nitrogen pipe network through a pipeline, a valve e, a one-way check valve c, a pipe cap-equipped pilot shower b, an 8-shaped blind plate c, a valve f and a pressure gauge d are sequentially arranged on the pipeline connected with the heat exchanger, the heat exchanger is communicated with a medium-pressure nitrogen gas phase through the pipeline, the pipeline connected with the heat exchanger is sequentially provided with the valve d, the pipe cap-equipped pilot shower valve a, the one-way check valve b, the pressure gauge b and a thermometer a, and the heat exchanger is a plate-fin heat exchanger and has a good effect.
Preferably: in order to facilitate the start-up, the system is further provided with a material flow a and a material flow b feeding pipeline, the material flow a and the material flow b are respectively communicated with the refrigerant suction tank 38 through pipelines, the connecting pipeline is provided with a stop valve a, a stop valve b, a stop valve c, an orifice plate flowmeter, a pressure gauge e, a thermometer b, a guide shower valve c with a pipe cap and a stop valve d, and the material flow a and the material flow b are selectively added through the stop valve a and the stop valve b.
Preferably: in order to ensure the safe operation of the system, a third safety valve group is arranged at the outlet of the heat exchanger, the first safety valve group comprises a valve g, a safety valve a, a valve h and a valve i, and the third safety valve group is connected to a flare gas pipe network through a pipeline.
Preferably: in order to facilitate the use of the system, a skid-mounted structure is designed in a square frame at the position A of the system, and a group of rollers are arranged at the lower part of the skid-mounted structure and used for moving the skid-mounted structure.
The detailed flow of the material flow a and the material flow b is as follows: the device comprises a refrigerant suction tank, a material flow a and a material flow b, wherein the material flow a and the material flow b are respectively communicated with the refrigerant suction tank through pipelines, a stop valve a, a stop valve b, a stop valve c, an orifice plate flowmeter, a pressure gauge e, a thermometer b, a guide shower valve c with a pipe cap and a stop valve d are arranged on the connected pipelines to realize the adjustment and monitoring of the material flow a and the material flow b, and the material flow a and the material flow b are selectively added through the stop valve a and the stop valve b.
The using method of the material flow a is that the material flow a is methane gas from an EOEG PSA unit purified by natural gas pressure swing adsorption, a stop valve b and a stop valve c are closed completely and a stop valve d is opened completely when feeding, the feeding speed is controlled by the opening degree of the stop valve a, the material flow state is detected by a pressure gauge e and a temperature gauge b, the expansion pressure displacement is realized by the upstream gas feeding of a guide shower valve c with a pipe cap and the material flow a, nitrogen is firstly displaced to below the dew point-60 ℃ and the oxygen content is lower than 0.02 vol% (the lower the dew point is the better if the field condition is good), then a connecting pipe is connected to a reserved port of a nearby pipe network, the nitrogen content of the material displacement is qualified, further, the change of the suction pressure and the temperature at one section of a refrigeration compressor is closely concerned when the material flow is connected, and the change of the pressure is concerned in real time and is introduced through the external material flow a, during the period, the balance adjustment can be carried out through the rotating speed of the compressor and the load of a user;
the material flow b is a gas phase component of a binary refrigeration system of a No. 1 light hydrocarbon cracking device or qualified methane effluent, the introduction method is similar to the material flow aa introduction method, only the stop valve b is operated to control the flow rate, the material flow b and the system belong to the same type of device to be introduced, the use and the investigation are most convenient, but more factories only build one set of light hydrocarbon cracking device and do not have comprehensive popularization value, and related flail heads can be reserved in the construction period to avoid the special operation of pressing and opening holes in the later period.
Stream a and stream b are significantly different in composition and cannot be simultaneously passed through a stop valve d because of common metering; further controlling the pressure of the material flow c to be 0.7-0.9 MPa, the temperature to be-30-45 ℃, controlling the pressure of the material flow a to be 0.5-0.6 MPa, the temperature to be 20-35 ℃ and the methane purity to be 98-99 mol%; the material exchange of the EOEG PSA unit and the methane-rich unit of the No. 1 light hydrocarbon cracking device can be realized in the opening states of the stop valve a and the stop valve b and the closing states of the stop valve c and the stop valve d of the material flow a and the material flow b, and the risk of the supply stability of the external natural gas of the EOEG PSA is reduced.
The shell heat exchange medium of the heat exchanger is MN (medium pressure nitrogen), the pressure is 3.5MPa, the gas phase is at a temperature slightly lower than the normal temperature, other equivalent media can be used, the tube pass is energy supply equipment for converting liquefied methane liquid phase into gas phase, the temperature is lower, and the media such as steam or factory wind with larger water content are not suitable to be used; furthermore, the heat exchanger is preferably in a high-efficiency plate-fin type, the cooling speed of the tube layer is required to be noticed in the application process, and the cooling speed is not required to exceed 35 ℃/hor; furthermore, the tube layer and the shell layer of the heat exchanger perform countercurrent heat exchange, and a multi-pass flow path is arranged through the partition plate so as to improve the heat exchange efficiency; furthermore, the heat exchanger shell medium leakage valve with the pipe cap can be used for tension-compression displacement discharge, dew point test and combustible gas test; further, after MN (medium-pressure nitrogen) passes through the heat exchanger, the components and the pressure are not changed, and MN (medium-pressure nitrogen) can be connected into an LN (low-pressure nitrogen) pipe network for continuous use, wherein the pressure is 0.6-0.8 MPa;
the material flow c is liquid-phase methane, and is easy to load and unload in a large amount, the material flow c can be combined into a skid-mounted structure by taking a flange as a boundary in the frame in the figure 2, so that the skid-mounted structure is easy to install, the space occupation ratio is further reduced, and a movable hub and a mounting structure can be carried, so that the skid-mounted structure can be further moved to other liquefied hydrocarbon gasification demand units after the binary refrigeration system is started, the condition that the utilization rate of long-term cold-backup fixed assets is low is reduced, and the 8-shaped blind plate b is inverted to a blind position after the binary refrigeration system is started;
liquid phase methane carried by the tank car is introduced into the suction tank through a heat exchanger, a valve and the like, the pressure of the suction tank is 20-80 KPa, the temperature is-80 to-130 ℃, the valve states along the pipeline are that the valve a is opened, the 8-shaped blind plate a is open, the blind cover pilot valve a is closed and the valve b is opened, the flow is controlled through the opening degree of the valve a, and the flow control reference is that the pressure gauge a, the pressure gauge b and the thermometer a display numerical values; furthermore, the dew point test of the flow path before use is lower than-60 ℃ and the oxygen content test is lower than 0.02 vol%, the purging, the replacement and the test can be carried out by connecting an air source outside a valve, and the air connecting point is not limited to the positions of the pipe cap leading shower b and the pipe cap leading shower a.
Before the equipment, the valve, the flange and the pipeline connection are put into use for the first time, a torch system, a fire-fighting system and a sis interlocking system are required to be put into use, the airtightness and pressure maintaining are qualified, the personnel evidence obtaining training is finished, the PSSR is required to be completely modified, a non-explosion-proof mobile phone cannot be carried on the equipment when the equipment enters the site, the inspection frequency of the inspection external operation is not lower than 1 h/time, a four-in-one detector is required to be carried, and the requirement is required to be not lower than the operation standard when the method is used;
the purpose of externally supplementing the binary refrigerant methane component can be realized by the material flow a, the material flow b and the material flow c, a user can use the binary refrigerant methane component according to the self site condition, further, the material flow a, the material flow b and the material flow c can be installed at one place, two places or three places simultaneously, further, the starting method of the binary refrigeration system is one step of the starting of the binary refrigeration system, and the method is put into use under the precondition that the motor drive or the turbine drive of the binary refrigeration system is started and the rotating speed is stable and adjustable; secondly, the starting of the single ethylene refrigerant is finished, and the suction pressure at the process side and the tail end discharge pressure of the compressor are stably operated; the content of carbon dioxide in the methane effluent of the separation unit is unqualified, and the separation temperature required by the demethanization unit cannot be reached in a short time; and fourthly, the field equipment is provided with a relevant reserved access port, the field combustible gas is completely monitored, the fire-fighting facilities are complete, and emergency measures are in place. The invention has the following advantages:
(1) by applying the method, the system improves the starting efficiency by introducing the binary refrigerant from the outside, reduces the emptying time of unqualified materials, thereby reducing the material consumption and energy consumption during the starting period, and reduces the cold loss without frequent impurity removal at the later stage because no impurity is introduced into the refrigerant in the starting process of the binary refrigeration system.
(2) By applying the method disclosed by the invention, the effect of quickly driving the vehicle can be achieved. The method reduces the conflict of the purification cold quantity of the residual ethane for supplementing pure methane by the carbon-separation of the binary refrigeration system and the self-demethanizing tower, takes a 125 ten thousand ton/year ethylene device as an example, and has the product value of 3000 ten thousand in a single day, and can lead the operation proportion of the secondary system refrigerant to reach the optimum in a plurality of days after the method is applied, thereby having higher potential economic value.
(3) The method can effectively reduce the potential risk of overload operation of the primary trace water removal dryer during the original start-up period, the running time of the trace water removal dryer is usually 48 hours, the carbon content of the regenerated gas is always higher within 48 hours during the start-up period, the pore diameter of the molecular sieve in the trace water removal dryer is limited, the unqualified regenerated gas is blindly desorbed and regenerated by the molecular sieve, the coking life of the molecular sieve of the dryer is greatly shortened, the refrigerating temperature reaches the standard after the binary refrigerant is in place in proportion, the content of the carbon-II of the hydrogen-rich material flowing out of the top of the demethanizer is fast qualified, the qualified hydrogen-rich regenerated gas is fast put into use, and the dryer is subjected to regeneration switching.
Drawings
FIG. 1 is a system diagram of the present invention
FIG. 2 is a second system diagram of the present invention.
Detailed Description
Example 1
As shown in fig. 1:
a binary refrigeration start system of a light hydrocarbon cracking device comprises a binary refrigeration system, wherein the binary refrigeration system comprises a refrigerant collecting tank 38, a compressor 37 and a user heat exchanger 46, the refrigerant collecting tank 38 is connected with the user heat exchanger 46 through a pipeline, the user heat exchanger 46 is connected with a refrigerant throttle valve 48 through a pipeline, a first safety valve set is arranged at a refrigerant outlet of the user heat exchanger 46, the first safety valve set comprises a first valve 33, a second valve 35, a third valve 36 and a safety valve b34, the first safety valve set is connected to a flare gas pipe network through a pipeline, the user heat exchanger 46 is connected with a refrigerant suction tank 38, one end of the compressor 37 is connected with the refrigerant suction tank 38 through a pipeline, the other end of the compressor 37 is communicated with a refrigerant collecting tank 52 through a pipeline, a liquid level meter a41 is installed on the refrigerant collecting tank 52, the second safety valve group, the cooling heat exchanger 50 and the thermometer 51 are sequentially installed on the connected pipeline, the second safety valve group comprises a fourth valve 45, a regulating valve 49, a fifth valve 47 and a safety valve c44, and the second safety valve group enters a flare gas pipe network through a pipeline, and the second safety valve group is characterized in that at least one logistics system is communicated with the refrigerant suction tank 38, the logistics system comprises a tank car 24 and a heat exchanger 29, a logistics c is installed in the tank car 24, the tank car 24 is communicated with the heat exchanger 29 through a pipeline, and the connected pipeline is sequentially provided with a valve a10, an 8-shaped blind plate a18, a blind cover guiding shower valve a1 and a valve b 12; the heat exchanger 29 is communicated with the refrigerant suction tank 38 through a pipeline, and the connected pipeline is sequentially provided with a pressure gauge a23, a one-way check valve a30, a blind cover pilot valve b31, an 8-shaped blind plate b32 and a valve c 40; the heat exchanger 29 is communicated with medium-pressure nitrogen through a pipeline, and a valve d24, a pilot valve a25 with a pipe cap, a one-way check valve b 26, a pressure gauge b27 and a thermometer a28 are sequentially arranged on the connected pipeline.
The heat exchanger 29 is communicated with a low-pressure nitrogen pipe network through a pipeline, a valve e11, a one-way check valve c13, a pipe cap-containing guide shower b14, an 8-shaped blind plate c15, a valve f16, a pressure gauge d17 and material flow a and material flow b feeding pipelines are sequentially arranged on the connected pipeline, the material flow a and the material flow b are respectively communicated with the refrigerant suction tank 38 through pipelines, a stop valve a2, a stop valve b4, the stop valve c3, an orifice plate flowmeter 5, a pressure gauge e6, a thermometer b7, a pipe cap-containing guide shower valve c9 and a stop valve d8 are arranged on the connected pipeline, the material flow a and the material flow b are selectively added through the stop valve a2 and the stop valve b4, the heat exchanger 29 is a plate-fin type heat exchanger, in order to ensure the safe operation of the system, a safety valve group III is arranged at the outlet of the heat exchanger 29, and the safety valve group I comprises a valve g19, a valve b 3538, a stop valve b 3583, a stop valve b4, a stop valve b3, a pressure gauge b3, a pressure gauge b gauge is selectively added by selecting one gauge and a gauge b gauge, A safety valve a20, a valve h21 and a valve i22, wherein the safety valve group III is connected to a flare gas pipe network through pipelines.
The working principle of the invention is as follows: the using method of the material flow a is that the material flow a is methane gas purified by natural gas pressure swing adsorption from an EOEG PSA unit, a stop valve b4 and a stop valve c3 are closed completely, a stop valve d8 is opened completely, the feeding speed is controlled by the opening degree of the stop valve a2, the material flow state is detected by a pressure gauge e6 and a temperature gauge b7, inflation pressure replacement is realized by feeding gas with a pipe cap guide shower valve c9 and the upstream of the material flow a, nitrogen is replaced to the dew point below-60 ℃ and the oxygen content is lower than 0.02 vol% (the lower the dew point is, the better the site condition is), then the material is connected to a reserved port of a nearby flare pipe network, the nitrogen content of the material replacement is qualified, further, the change of the suction pressure and temperature at one section of a refrigeration compressor is closely paid attention when the material flow is connected, and the change of the pressure is paid attention in real time to be introduced through the external material flow a smoothly, during the period, the balance adjustment can be carried out through the rotating speed of the compressor and the load of a user.
The material flow b is a gas phase component of a binary refrigeration system of a No. 1 light hydrocarbon cracking device or qualified methane effluent, the introduction method is similar to the material flow a introduction method, only a stop valve b4 is operated to control the flow rate, the material flow b and the system belong to the same type of device to be introduced, the use and the investigation are most convenient, but more factories only build one set of light hydrocarbon cracking device and do not have comprehensive popularization value, and related swing heads can be kept in the construction period to avoid the special operation of pressing and opening holes in the later period.
Stream a and stream b are significantly different in composition and cannot flow through the stop valve d at the same time due to public metering; further controlling the pressure of the material flow c to be 0.7-0.9 MPa, the temperature to be-30-45 ℃, controlling the pressure of the material flow a to be 0.5-0.6 MPa, the temperature to be 20-35 ℃ and the methane purity to be 98-99 mol%; the material exchange of the EOEG PSA unit and the methane-rich unit of the 1# light hydrocarbon cracking unit can be realized in the opening states of the stop valve a2 and the stop valve b4 and the closing states of the stop valve c3 and the stop valve d8 of the material flow a and the material flow b, and the risk of supplying stability of natural gas outside the EOEG PSA is reduced.
The shell heat exchange medium of the heat exchanger 29 is MN (medium pressure nitrogen), the pressure is 3.5MPa, the gas phase is at a temperature slightly lower than the normal temperature, other equivalent media can be used, the tube pass is energy supply equipment for converting liquefied methane liquid phase into gas phase, the temperature is lower, and media such as steam or factory wind with larger water content are not suitable to be used; furthermore, the heat exchanger is preferably in a high-efficiency plate-fin type, the temperature reduction speed of the tube layer is required to be noticed in the application process, and the temperature reduction speed is recommended to be not more than 35 ℃/hor; furthermore, the tube layer and the shell layer of the heat exchanger 29 are used for countercurrent heat exchange, and a multi-pass flow path is arranged through the partition plates so as to improve the heat exchange efficiency; furthermore, the heat exchanger shell medium leakage valve with the pipe cap can be used for tension-compression displacement discharge, dew point test and combustible gas test; further, after MN passes through the heat exchanger, the components and the pressure of MN are not changed, and MN can be connected into an LN (low-pressure nitrogen) pipe network for continuous use, and the pressure is 0.6-0.8 MPa.
Example 2
As shown in fig. 2:
a binary refrigeration start system of a light hydrocarbon cracking device comprises a binary refrigeration system, wherein the binary refrigeration system comprises a refrigerant collecting tank 38, a compressor 37 and a user heat exchanger 46, the refrigerant collecting tank 38 is connected with the user heat exchanger 46 through a pipeline, the user heat exchanger 46 is connected with a refrigerant throttle valve 48 through a pipeline, a first safety valve group is arranged at a refrigerant outlet of the user heat exchanger 46, the first safety valve group comprises a first valve 33, a second valve 35, a third valve 36 and a safety valve b34, the first safety valve group is connected to a flare gas pipe network through a pipeline, one end of the compressor 37 is connected with a refrigerant suction tank 38 through a pipeline, the other end of the compressor 37 is communicated with a refrigerant collecting tank 52 through a pipeline, a liquid level meter a41 is installed on the refrigerant collecting tank 52, and the second safety valve group, the second safety valve group and the first safety valve group are sequentially installed on the pipeline, The cooling heat exchanger 50 and the thermometer 51, the second safety valve group includes valve four 45, regulating valve 49, valve five 47 and safety valve c44, the second safety valve group enters the flare gas pipe network through the pipeline, characterized in that, the refrigerant suction tank 38 at least connects a material flow system, the material flow system includes the tank car 24 and the heat exchanger 29, the tank car 24 is equipped with material flow c, the tank car 24 and the heat exchanger 29 are connected through the pipeline, the connecting pipeline is equipped with valve a10, 8-shaped blind plate a18, blind cover pilot shower valve a1 and valve b12 in turn; the heat exchanger 29 is communicated with the refrigerant suction tank 38 through a pipeline, and a pressure gauge a23, a one-way check valve a30, a blind cover pilot valve b31, an 8-shaped blind plate b32 and a valve c40 are sequentially arranged on the connected pipeline; the heat exchanger 29 is communicated with medium-pressure nitrogen through a pipeline, and a valve d24, a pipe-cap-equipped shower guide valve a25, a one-way check valve b 26, a pressure gauge b27 and a thermometer a28 are sequentially arranged on the connected pipeline.
The heat exchanger 29 is communicated with a low-pressure nitrogen pipe network through a pipeline, a valve e11, a one-way check valve c13, a pipe cap-equipped guide shower b14, an 8-shaped blind plate c15, a valve f16, a pressure meter d17, a material flow a feeding pipeline and a material flow b feeding pipeline are sequentially arranged on the connecting pipeline, the material flow a and the material flow b are respectively communicated with the refrigerant suction tank 38 through pipelines, a stop valve a2, a stop valve b4, a stop valve c3, an orifice plate flowmeter 5, a pressure meter e6, a thermometer b7, a pipe cap-equipped guide shower valve c9 and a stop valve d8 are arranged on the connecting pipeline, the material flow a and the material flow b are selectively added through one of the stop valve a2 and the stop valve b4, the heat exchanger 29 is a plate-fin heat exchanger, in order to ensure the safe operation of the system, a safety valve group III is arranged at the outlet of the heat exchanger 29, the safety valve group I comprises a valve g19, a valve g, a valve b 35, a pressure meter b3, a pressure meter and a pressure meter, a pressure meter, a pressure meter, a pressure meter, a meter, a safety valve a20, a valve h21 and a valve i22, wherein the safety valve group III is connected to a flare gas pipe network through pipelines.
The working principle of the invention is as follows: the using method of the material flow a is that the material flow a is methane gas purified by natural gas pressure swing adsorption from an EOEG PSA unit, a stop valve b4 and a stop valve c3 are closed completely, a stop valve d8 is opened completely, the feeding speed is controlled by the opening degree of the stop valve a2, the material flow state is detected by a pressure gauge e6 and a temperature gauge b7, inflation pressure replacement is realized by feeding gas with a pipe cap guide shower valve c9 and the upstream of the material flow a, nitrogen is replaced to the dew point below-60 ℃ and the oxygen content is lower than 0.02 vol% (the lower the dew point is, the better the site condition is), then the material is connected to a reserved port of a nearby flare pipe network, the nitrogen content of the material replacement is qualified, further, the change of the suction pressure and temperature at one section of a refrigeration compressor is closely paid attention when the material flow is connected, and the change of the pressure is paid attention in real time to be introduced through the external material flow a smoothly, during the period, the balance adjustment can be carried out through the rotating speed of the compressor and the load of a user;
the material flow b is a gas phase component of a binary refrigeration system of a No. 1 light hydrocarbon cracking device or qualified methane effluent, the introduction method is similar to the material flow a introduction method, only a stop valve b4 is operated to control flow rate, the material flow b and the system belong to the same type of device to be introduced, the use and the investigation are most convenient, but more factories only build one set of light hydrocarbon cracking device and do not have comprehensive popularization value, and related swinging heads can be kept in the construction period to avoid special operations of pressing and opening holes in the later period.
Stream a and stream b are significantly different in composition and cannot be simultaneously passed through a stop valve d because of common metering; further controlling the pressure of the material flow c to be 0.7-0.9 MPa, the temperature to be-30-45 ℃, controlling the pressure of the material flow a to be 0.5-0.6 MPa, the temperature to be 20-35 ℃ and the methane purity to be 98-99 mol%; the material exchange of the EOEG PSA unit and the methane-rich unit of the 1# light hydrocarbon cracking unit can be realized in the opening states of the stop valve a2 and the stop valve b4 and the closing states of the stop valve c3 and the stop valve d8 of the material flow a and the material flow b, and the risk of supplying stability of natural gas outside the EOEG PSA is reduced.
The shell heat exchange medium of the heat exchanger 29 is MN (medium pressure nitrogen), the pressure is 3.5MPa, the gas phase is at a temperature slightly lower than the normal temperature, other equivalent media can be used, the tube pass is energy supply equipment for converting liquefied methane liquid phase into gas phase, the temperature is lower, and media such as steam or factory wind with larger water content are not suitable to be used; furthermore, the heat exchanger is preferably in a high-efficiency plate-fin type, the temperature reduction speed of the tube layer is required to be noticed in the application process, and the temperature reduction speed is recommended to be not more than 35 ℃/hor; further, the tube layer and the shell layer of the heat exchanger 29 are used for countercurrent heat exchange, and a multi-pass flow path is arranged through the partition plates so as to improve the heat exchange efficiency; furthermore, the heat exchanger shell medium leakage valve with the pipe cap can be used for tension-compression displacement discharge, dew point test and combustible gas test; further, after the MN passes through the heat exchanger, the components and the pressure of the MN are not changed, and the MN can be connected into an LN (low-pressure nitrogen) pipe network for continuous use, wherein the pressure is 0.6-0.8 MPa. A square frame at the position A of the system is designed into a skid-mounted structure, and a group of rollers for the skid-mounted structure to move are arranged at the lower part of the skid-mounted structure.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that modifications can be made by those skilled in the art without departing from the principle of the present invention, and these modifications should also be construed as the protection scope of the present invention.
Claims (6)
1. A binary refrigeration starting system of a light hydrocarbon cracking device comprises a binary refrigeration system, wherein the binary refrigeration system comprises a refrigerant suction tank (38), a compressor (37) and a user heat exchanger (46), the refrigerant suction tank (38) is connected with the user heat exchanger (46) through a pipeline, the user heat exchanger (46) is connected with a refrigerant throttle valve (48) through a pipeline, a first safety valve group is arranged at a refrigerant outlet of the user heat exchanger (46), the first safety valve group comprises a first valve (33), a second valve (35), a third valve (36) and a safety valve b (34), the first safety valve group is connected to a flare gas pipe network through a pipeline, one end of the compressor (37) is connected with the refrigerant suction tank (38) through a pipeline, a remote transmission thermometer (42) and a remote transmission pressure gauge (43) are installed on the connected pipeline, and the other end of the compressor (37) is communicated with a refrigerant collecting tank (52) through a pipeline, the refrigerant collecting tank (52) is provided with a liquid level meter a (41), the connecting pipeline is sequentially provided with a second safety valve group, a cooling heat exchanger (50) and a thermometer (51), the second safety valve group comprises a fourth valve (45), a regulating valve (49), a fifth valve (47) and a safety valve c (44), and the second safety valve group enters a torch gas pipe network through a pipeline,
the refrigerant suction tank (38) is communicated with a logistics system c, the logistics system c comprises a tank car (24) and a heat exchanger (29), the logistics c is installed in the tank car (24), the tank car (24) is communicated with the heat exchanger (29) through a pipeline, and a valve a (10), an 8-shaped blind plate a (18), a blind cover pilot valve a (1) and a valve b (12) are sequentially arranged on the connected pipeline;
the heat exchanger (29) is communicated with a refrigerant suction tank (38) through a pipeline, and a pressure gauge a (23), a one-way check valve a (30), a blind cover pilot valve b (31), an 8-shaped blind plate b (32) and a valve c (40) are sequentially arranged on the connected pipeline;
one end of the heat exchanger (29) is communicated with a low-pressure nitrogen pipe network through a pipeline, and a valve e (11), a one-way check valve c (13), a pilot shower valve b (14) with a pipe cap, an 8-shaped blind plate c (15), a valve f (16) and a pressure gauge d (17) are sequentially arranged on the connected pipeline;
the other end of the heat exchanger (29) is communicated with medium-pressure nitrogen through a pipeline, and a valve d (24), a pilot valve a (25) with a pipe cap, a one-way check valve b (26), a pressure gauge b (27) and a thermometer a (28) are sequentially arranged on the connected pipeline.
2. The binary refrigeration start system of a light hydrocarbon cracking device according to claim 1, characterized in that a material flow a and a material flow b feeding pipeline are further provided, the material flow a and the material flow b are respectively communicated with the refrigerant suction tank (38) through pipelines, the connecting pipeline is provided with a stop valve a (2), a stop valve b (4), a stop valve c (3), an orifice plate flowmeter (5), a pressure gauge e (6), a thermometer b (7), a pipe cap guiding valve c (9) and a stop valve d (8), wherein the material flow a and the material flow b are selectively added through the stop valve a (2) and the stop valve b (4).
3. The binary refrigeration system for driving a light hydrocarbon cracking device according to claim 1, wherein the heat exchanger (29) is a plate-fin heat exchanger.
4. The binary refrigeration methane make-up system of a light hydrocarbon cracking device according to claim 1, wherein a third relief valve set is arranged at the outlet of the heat exchanger (29), the first relief valve set comprises a valve g (19), a relief valve a (20), a valve h (21) and a valve i (22), and the third relief valve set is connected to a flare gas pipe network through a pipeline.
5. The binary refrigeration driving system of the light hydrocarbon cracking device, as set forth in claim 1, wherein the inside of the frame at the position of the system a is designed to be a skid-mounted structure, and a set of rollers is provided at the lower part of the skid-mounted structure for the skid-mounted structure to move.
6. A start-up method of a binary refrigeration start-up system of a light hydrocarbon cracking device is characterized by comprising the following steps:
1) the operation is performed in the preorder, the motor drive or the turbine drive of the binary refrigeration system is started, and the rotating speed is stable and adjustable; the start of the single ethylene refrigerant is finished, and the process side suction pressure and the tail end discharge pressure of the compressor stably operate; the content of carbon dioxide in the methane effluent of the separation unit is unqualified, and the separation temperature required by the demethanization unit cannot be reached in a short time; the field equipment is provided with a relevant reserved access port, the field combustible gas is completely monitored, the fire-fighting facilities are complete, and emergency measures are in place;
2) liquid-phase methane carried by a tank car (24) is a material flow c, the material flow c is introduced into a refrigerant suction tank (38) through a heat exchanger (29) and a valve, the pressure of the refrigerant suction tank (38) is 20-80 KPa, the temperature is-80-130 ℃, the states of valves along the pipeline are that the valve a (10) is opened, the 8-shaped blind plate a (18) is opened, the blind cover pilot valve a (1) is closed and the valve b (12) is opened, the flow is controlled through the opening degree of the valve a (10), the flow control references are a pressure gauge a (23), a pressure gauge b (27) and a temperature gauge a (28) display dew point, the testing temperature of the flow is lower than-60 ℃ before the flow is put into service, the testing of the oxygen content is lower than 0.02%, the purging, the replacement and the testing can be carried out through an external air source of the valve, and the air receiving point is not limited to the positions of a pipe cap pilot valve b (14) and a pipe cap pilot valve a (25);
3) the purpose of externally supplementing binary refrigerant methane components is realized by material flow a, material flow b and material flow c, a user can use the methane gas according to the self site condition, the material flow a, the material flow b and the material flow c can be installed at one position, two positions or three positions simultaneously, the material flow a is the methane gas purified by natural gas pressure swing adsorption from an EOEGPSA unit, a stop valve b (4) and a stop valve c (3) are fully closed during feeding, a stop valve d (8) is fully opened, the feeding speed is controlled by the opening degree of the stop valve a (2), the state of the material flow a is detected by a pressure gauge e (6) and a temperature gauge b (7), the expansion pressure displacement is realized by the guide shower valve c (9) with a pipe cap and the gas feeding at the upstream of the material flow a, the nitrogen displacement is firstly carried out to the dew point below 60 ℃ below the dew point and the oxygen content is lower than 0.02 vol%, then the reserved port of a nearby flare pipe network is connected to ensure that the nitrogen content of the material displacement is qualified, furthermore, when the material flow is accessed, the change of a section of suction pressure and temperature of the refrigeration compressor (37) should be closely concerned, the change of the pressure is concerned in real time to be led in through the external material flow a, and the balance adjustment is carried out through the rotating speed of the compressor (37) and the load of a user; the material flow b is a gas phase component of a binary refrigeration system of a No. 1 light hydrocarbon cracking device or qualified methane effluent, the introduction method is similar to the material flow a introduction method, only a stop valve b (4) is controlled to control the flow, the material flow b and the system belong to the same type of device to be led out, and the material flow a and the material flow b have obvious component difference and cannot simultaneously flow through a stop valve d (8) due to public metering; the pressure of the material flow c is controlled to be 0.7-0.9 MPa, the temperature is controlled to be-30-45 ℃, the pressure of the material flow a is controlled to be 0.5-0.6 MPa, the temperature is controlled to be 20-35 ℃, and the purity of methane is 98-99 mol%; the material exchange of the EOEGPSA unit and a methane-rich unit of a No. 1 light hydrocarbon cracking device is realized in the opening states of a stop valve a (2) and a stop valve b (4) and the closing states of a stop valve c (3) and a stop valve d (8) of the material flows a and b; the shell heat exchange medium of the heat exchanger (29) is MN (medium-pressure nitrogen), the pressure is 3.5MPa, the gas phase and the temperature are slightly lower than the normal temperature, the components and the pressure of MN (medium-pressure nitrogen) are not changed after passing through the heat exchanger, LN (low-pressure nitrogen) pipe network is accessed for continuous use, the pressure is 0.6-0.8 MPa, the system A is designed to be of a skid-mounted structure in a square frame, and the lower part of the skid-mounted structure is provided with a group of rollers for moving the skid-mounted structure.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1164890A (en) * | 1994-11-08 | 1997-11-12 | 威廉斯菲尔德服务公司 | LNG production in cryogenic natural gas processing plants |
| US5979177A (en) * | 1998-01-06 | 1999-11-09 | Abb Lummus Global Inc. | Ethylene plant refrigeration system |
| CN104713310A (en) * | 2015-03-11 | 2015-06-17 | 新奥气化采煤有限公司 | Methane gas recycling system and recycling control method |
| CN106831291A (en) * | 2017-01-05 | 2017-06-13 | 中石化上海工程有限公司 | The method of Catalyst for Oxidative Coupling of Methane |
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