CN117804255B - Heat exchange station system for comprehensive utilization of cold energy - Google Patents
Heat exchange station system for comprehensive utilization of cold energy Download PDFInfo
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- CN117804255B CN117804255B CN202311658269.4A CN202311658269A CN117804255B CN 117804255 B CN117804255 B CN 117804255B CN 202311658269 A CN202311658269 A CN 202311658269A CN 117804255 B CN117804255 B CN 117804255B
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- 239000000463 material Substances 0.000 claims abstract description 145
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 103
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 99
- 238000003860 storage Methods 0.000 claims abstract description 47
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 160
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 88
- 239000005977 Ethylene Substances 0.000 claims description 88
- 239000001294 propane Substances 0.000 claims description 80
- 239000002131 composite material Substances 0.000 claims description 37
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 20
- 150000001875 compounds Chemical class 0.000 claims description 14
- LYCAIKOWRPUZTN-UHFFFAOYSA-N ethylene glycol Natural products OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims description 11
- 238000007710 freezing Methods 0.000 claims description 11
- 230000008014 freezing Effects 0.000 claims description 11
- 229910052757 nitrogen Inorganic materials 0.000 claims description 10
- 238000012544 monitoring process Methods 0.000 claims description 4
- 239000007788 liquid Substances 0.000 claims description 3
- 238000007789 sealing Methods 0.000 claims description 3
- 230000001502 supplementing effect Effects 0.000 claims description 3
- 238000003466 welding Methods 0.000 claims description 3
- 125000003827 glycol group Chemical group 0.000 claims description 2
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims description 2
- 238000003303 reheating Methods 0.000 abstract description 6
- 230000002457 bidirectional effect Effects 0.000 abstract description 2
- 238000004519 manufacturing process Methods 0.000 description 11
- 230000005465 channeling Effects 0.000 description 10
- 238000000034 method Methods 0.000 description 8
- 230000008569 process Effects 0.000 description 8
- 230000008901 benefit Effects 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- 230000008859 change Effects 0.000 description 3
- 230000001276 controlling effect Effects 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000007711 solidification Methods 0.000 description 3
- 230000008023 solidification Effects 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 230000005856 abnormality Effects 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000009365 direct transmission Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000009991 scouring Methods 0.000 description 1
- 230000001960 triggered effect Effects 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D9/00—Heat-exchange apparatus having stationary plate-like or laminated conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D1/00—Pipe-line systems
- F17D1/08—Pipe-line systems for liquids or viscous products
- F17D1/082—Pipe-line systems for liquids or viscous products for cold fluids, e.g. liquefied gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D1/00—Pipe-line systems
- F17D1/08—Pipe-line systems for liquids or viscous products
- F17D1/14—Conveying liquids or viscous products by pumping
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D3/00—Arrangements for supervising or controlling working operations
- F17D3/01—Arrangements for supervising or controlling working operations for controlling, signalling, or supervising the conveyance of a product
-
- 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
- F25D—REFRIGERATORS; COLD ROOMS; ICE-BOXES; COOLING OR FREEZING APPARATUS NOT OTHERWISE PROVIDED FOR
- F25D17/00—Arrangements for circulating cooling fluids; Arrangements for circulating gas, e.g. air, within refrigerated spaces
- F25D17/02—Arrangements for circulating cooling fluids; Arrangements for circulating gas, e.g. air, within refrigerated spaces for circulating liquids, e.g. brine
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Public Health (AREA)
- Water Supply & Treatment (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Sorption Type Refrigeration Machines (AREA)
Abstract
The invention discloses a heat exchange station system for comprehensively utilizing cold energy, which comprises a first low-temperature material source, a second low-temperature material source, a liquid ammonia source and a chilled water pipeline network, wherein the first low-temperature material source is connected to a first low-temperature material reheater through a first low-temperature material preheater, and the liquid ammonia source is respectively connected with the first low-temperature material preheater and the second low-temperature material preheater through two heat source output branches and is connected to a low-temperature liquid ammonia storage tank; the second low-temperature material source is respectively connected to the first low-temperature material preheater and the second low-temperature material preheater through two cold source output branches, and is connected to the second low-temperature material reheater, and the chilled water pipe network is connected to the second low-temperature material preheater through a chilled water storage tank and a chilled water circulating pump and then connected back to the chilled water pipe network. The invention fully utilizes the cold energy of the low-temperature material, realizes bidirectional heat exchange, reduces the temperature of liquid ammonia pouring, increases the pouring amount in unit time, and improves the temperature of the low-temperature material before reheating and external transportation.
Description
Technical Field
The invention belongs to the technical field of low-temperature liquid storage, and particularly relates to a heat exchange station system for comprehensively utilizing cold energy.
Background
The modern large petrochemical industry is often matched with a low-temperature storage tank area with larger construction scale, for example, materials stored in the low-temperature tank area of my department cover low-temperature ethylene (-102 ℃), low Wen Bingwan (-42 ℃) and low Wen Yean (-33 ℃), and the main process is that the low-temperature materials are subjected to reheating and are externally conveyed to various production devices. The raw material purchasing is divided into two modes of unloading ship and unloading by the influence of the price of the inner disk and the outer disk of the liquid ammonia, when the price of the inner disk is lower, the liquid ammonia purchasing is mainly based on normal-temperature liquid ammonia unloading, 4 unloading crane positions are arranged in the low-temperature tank area of the department of I, and 2 seats of the liquid ammonia spherical tank are used for receiving and unloading liquid ammonia tank trucks. The capacity of the existing normal-temperature liquid ammonia pouring and feeding low-temperature liquid ammonia storage tank is about 8t/h, the pouring capacity is low, the liquid ammonia unloading requirement cannot be met, and the electricity consumption of a BOG re-liquefying system of the low-temperature storage tank is greatly increased due to the pouring working condition.
The materials stored in the low-temperature storage tank areas are rich in cold energy, so that the cold energy can be effectively recovered and comprehensively utilized, and obvious energy-saving and emission-reducing benefits can be obtained. Therefore, the cold energy before recovering the low-temperature ethylene and reheating the low Wen Bingwan is used for freezing the normal-temperature liquid ammonia and pouring the normal-temperature liquid ammonia into the low-temperature tank, so that the pouring capability of the normal-temperature liquid ammonia is obviously improved and the energy consumption is reduced. However, the low-temperature materials in the low-temperature storage tank area are required to be reheated at a relatively stable temperature and then output, so that the output temperature control of the low-temperature materials and the conveying amount and the temperature control of liquid ammonia pouring are required to be considered simultaneously when cold energy utilization is carried out, and therefore, the high-controllability requirement on cold energy utilization is provided.
Meanwhile, materials stored in the low-temperature tank are basically device production raw materials, when different media are subjected to material channeling in the hot handover process, serious quality accidents can be caused, and the production safety and stability of downstream devices are greatly influenced, so that the cold energy recovery is required to fully evaluate the material channeling risk and design precautionary measures. Finally, besides liquid ammonia, devices such as temperature control equipment of the low-temperature storage tank area can also generate circulating water (chilled water), the temperature of the circulating water is higher when the circulating water is output from the corresponding equipment, and an ice maker needs to be started to refrigerate the circulating water, so that the circulating water is accompanied with cooling for corresponding materials. The operation of these ice machines also generates a great deal of energy consumption, which can be further reduced if cold energy of low-temperature materials is utilized.
Disclosure of Invention
The invention aims to provide a heat exchange station system for comprehensively utilizing cold energy, so as to solve the technical problems that the prior art lacks the cold energy utilization of low-temperature materials in the liquid ammonia pouring process, and the output temperature of the low-temperature materials, the incremental temperature control of the liquid ammonia pouring and other requirements are difficult to ensure simultaneously.
The heat exchange station system for comprehensively utilizing cold energy comprises a first low-temperature material source, a second low-temperature material source, a liquid ammonia source, a chilled water pipe network, a first low-temperature material reheater, a second low-temperature material reheater, a low Wen Yean storage tank, a first low-temperature material preheater, a second low-temperature material preheater and a chilled water storage tank, wherein the first low-temperature material source is connected with a cold source inlet of the first low-temperature material preheater through a first pipeline, a cold source outlet of the first low-temperature material preheater is connected with an inlet of the first low-temperature material reheater through a second pipeline, the liquid ammonia source is connected with an inlet of a third pipeline, the third pipeline is provided with two heat source output branches, outlets of the two heat source output branches are respectively connected with a heat source inlet of the first low-temperature material preheater and a heat source inlet of the second low-temperature material preheater, the low-temperature liquid ammonia storage tank is connected with the outlet of a fourth pipeline, the fourth pipeline is provided with two heat source input branches, the heat source outlet of the first low-temperature material preheater and the heat source outlet of the second low-temperature material preheater are respectively connected with the inlets of the two heat source input branches, the second low-temperature material source is connected with the inlet of a fifth pipeline, the fifth pipeline is provided with two cold source output branches, the outlets of the two cold source output branches are respectively connected with the cold source inlet of the first low-temperature material preheater and the cold source inlet of the second low-temperature material preheater, the inlet of the second low-temperature material reheater is connected with a sixth pipeline, the sixth pipeline is provided with two cold source input branches, the cold source outlet of the first low-temperature material preheater and the cold source outlet of the second low-temperature material preheater are respectively connected with the inlets of the two cold source input branches, the chilled water pipe network is connected with the chilled water storage tank through a chilled water output pipe, the chilled water storage tank is connected with a seventh pipeline, the seventh pipeline is connected to the heat source inlet of the second low-temperature material preheater through the chilled water circulating pump, and the heat source outlet of the second low-temperature material preheater is connected back to the chilled water pipe network through the chilled water circulating pipe.
Preferably, the first low-temperature material is low-temperature ethylene, and the second low-temperature material is low Wen Bingwan; the first low-temperature material source is a low-temperature ethylene storage tank and an ethylene feed pump, the second low-temperature material source is a low-temperature propane storage tank and a propane feed pump, the reheaters are respectively a corresponding ethylene reheater and a corresponding propane reheater, the preheaters are respectively a corresponding ethylene preheater, a corresponding propane preheater I and a corresponding propane preheater II, and the liquid ammonia source is a liquid ammonia tank car or a liquid ammonia spherical tank and a corresponding liquid ammonia feed pump.
Preferably, the ethylene preheater adopts a double composite heat exchanger structure, and comprises an upper composite heat exchanger and a lower composite heat exchanger, wherein the lower composite heat exchanger is provided with a heat source inlet and a heat source outlet of the ethylene preheater, normal-temperature liquid ammonia enters a tube pass of the lower composite heat exchanger through the heat source inlet, the upper composite heat exchanger is provided with a cold source inlet and a cold source outlet of the ethylene preheater, low-temperature ethylene enters the tube pass of the upper composite heat exchanger through the cold source inlet, a shell pass of the upper composite heat exchanger is communicated with a shell pass of the lower composite heat exchanger, and heat exchange media are arranged in the two shell passes, wherein the heat exchange media are propane in the embodiment.
Preferably, the first propane preheater and the second propane preheater have the same structure and are double-tube plate heat exchangers; the double-tube plate type heat exchanger comprises an inner tube plate, a tube bundle and an outer tube plate, wherein the inner tube plate is sealed with the tube bundle through expansion joint, the outer tube plate is sealed with the tube bundle through welding, a cavity is formed between the inner tube plate and the outer tube plate, nitrogen is filled in the cavity to maintain pressure, a pressure transmitter is arranged in the cavity, the pressure maintaining pressure is 0.6MPa, and the pressure transmitter is used for monitoring leakage of joints of the tube bundle and the tube plate.
Preferably, the first pipeline, the two heat source output branches and the two cold source output branches are all provided with control valves for controlling the opening and closing of the pipeline and the flow of materials in the pipeline.
Preferably, the ethylene preheater is further provided with autonomous interlock logic as follows:
Interlock logic one: when the shell side temperature of the upper composite heat exchanger is lower than-65 ℃, the control valve on the first pipeline and the control valve on the corresponding heat source output pipeline are closed in an interlocking way, the cold source input and the heat source input of the ethylene preheater are cut off, and meanwhile, the direct pipeline is opened to enable low-temperature ethylene to be directly input into the ethylene reheater;
And interlocking logic II: when the temperature of the heat source outlet of the lower compound heat exchanger is lower than-40 ℃, the control valve on the first pipeline and the control valve on the corresponding heat source output pipeline are closed in an interlocking way, the cold source input and the heat source input of the ethylene preheater are cut off, and meanwhile, the direct transmission pipeline is opened to enable low-temperature ethylene to be directly input into the ethylene reheater;
interlocking logic three: when the outlet pressure of the cold source of the upper composite heat exchanger is higher than 2.8Mpa, the control valve on the corresponding heat source output pipeline is closed in an interlocking way, and the heat source input of the ethylene preheater is cut off.
Preferably, the chilled water is glycol water solution with the content of 55%, nitrogen sealing measures are designed for the chilled water tank, a pressure reducing valve is arranged on a nitrogen supplementing pipeline to maintain constant tank pressure, and in order to prevent the chilled water pump from being evacuated, the system is also provided with self-control interlocking logic: the interlock stops the chilled water circulation pump when the chilled water level in the chilled water storage tank is below a threshold.
Preferably, the temperature of the liquid ammonia at normal temperature is 25 ℃, the temperature of chilled water output by a chilled water pipe network is 12 ℃, and the temperature of ethylene input into an ethylene reheater is-53 ℃; in a stable state, the temperature of propane output from the first propane preheater to the propane reheater is-11.6 ℃, the temperature of propane output from the second propane preheater to the propane reheater is-14 ℃, and the temperature of chilled water output from the second propane preheater is 7 ℃; the temperature of the liquid ammonia input into the low-temperature liquid ammonia storage tank by the ethylene preheater is minus 25 ℃, and the temperature of the liquid ammonia input into the low-temperature liquid ammonia storage tank by the propane preheater is minus 6.6 ℃.
The invention has the following advantages: the invention fully collects and recycles the cold energy of the low-temperature materials through the combined operation of the system, thereby realizing the maximization of energy-saving benefit; the heat exchangers of the system can be independently operated or can be operated in a combined mode, the operation is flexible, and the operation modes are various. When the system is operated in a combined mode, the 4 different mediums exchange heat pairwise and are then delivered to a downstream device. The cold energy of the low-temperature materials is fully utilized, the bidirectional heat exchange is realized, the temperature of liquid ammonia pouring is reduced, the pouring amount in unit time is increased, the temperature of the low-temperature materials before the reheating and external conveying is improved, and remarkable energy-saving and emission-reducing benefits are generated. In a specific embodiment, the capacity of realizing that normal-temperature liquid ammonia is poured into a low-temperature liquid ammonia tank is improved from 8t/h to 25t/h, and the electricity consumption generated by pouring normal-temperature liquid ammonia is reduced by about 88 ten thousand KWH/ten thousand tons; meanwhile, the cold energy of the storage tank is provided for replacing the running of the ice machine, the low-temperature materials are effectively utilized to reduce the temperature of the chilled water output after heat tracing, and the power consumption is reduced by about 135 ten thousand KWH each year.
On the other hand, because the conveyed low-temperature materials are easy to leak and blow-by, when the preheater is arranged, the double-tube plate type heat exchanger is adopted, so that the risk of low Wen Bingwan and normal-temperature liquid ammonia blow-by is effectively reduced. Aiming at the problem that the temperature of ethylene is lower and the freezing of liquid ammonia possibly occurs, the corresponding ethylene preheater adopts an upper composite heat exchanger and a lower composite heat exchanger to avoid the freezing of the liquid ammonia by introducing heat exchange medium propane, and meanwhile, the problem of leakage and channeling between ethylene and the liquid ammonia is also avoided.
Finally, the system adopts corresponding self-control interlocking logic and corresponding process parameter adjustment modes, thereby avoiding production faults such as solidification of liquid ammonia, brittle fracture of pipelines, overhigh expansion pressure of pipelines, evacuation of a chilled water pump and the like, realizing adjustment of only a single process parameter when the system is adjusted, and avoiding production fluctuation caused by simultaneous adjustment of two or more variable variables by the system.
Drawings
Fig. 1 is a schematic structural diagram of a heat exchange station system for comprehensive utilization of cold energy according to the present invention.
Fig. 2 is a schematic diagram of the relevant parts of the ethylene preheater in the present invention.
Fig. 3 is a schematic diagram of a related portion of a propane preheater according to the present invention.
Fig. 4 is a schematic diagram of the structure of the relevant part of the propane preheater in the present invention.
Fig. 5 is a schematic view of a double tube plate heat exchanger according to the present invention.
Reference numerals in the drawings include: 1. ethylene preheater, 2, propane preheater, 3, propane preheater, 4, chilled water storage tank, 5, chilled water circulation pump, 6, first pipeline, 7, second pipeline, 8, third pipeline, 9, fourth pipeline, 10, fifth pipeline, 11, sixth pipeline, 12, chilled water output pipe, 13, seventh pipeline, 14, chilled water circulation pipe, 15, lower composite heat exchanger, 16, upper composite heat exchanger, 17, ethylene reheater, 18, low Wen Yixi storage tank, 19, propane reheater, 20, low Wen Bingwan storage tank, 21, outer pipe plate, 22, inner pipe plate, 23, chamber.
Detailed Description
The following detailed description of the embodiments of the invention, given by way of example only, is presented in the accompanying drawings to aid in a more complete, accurate, and thorough understanding of the inventive concepts and aspects of the invention by those skilled in the art.
As shown in fig. 1-5, the invention provides a heat exchange station system for comprehensively utilizing cold energy, which comprises a first low-temperature material source, a second low-temperature material source, a liquid ammonia source, a chilled water pipe network, a first low-temperature material reheater, a second low-temperature material reheater, a low Wen Yean storage tank, a first low-temperature material preheater, a second low-temperature material preheater I, a second low-temperature material preheater II and a chilled water storage tank 4, wherein the first low-temperature material source is connected with a cold source inlet of the first low-temperature material preheater through a first pipeline 6, a cold source outlet of the first low-temperature material preheater is connected with an inlet of the first low-temperature material reheater through a second pipeline 7, the liquid ammonia source is connected with an inlet of a third pipeline 8, the third pipeline 8 is provided with two heat source output branches, outlets of the two heat source output branches are respectively connected with a heat source inlet of the first low-temperature material preheater and a heat source inlet of the second low-temperature material preheater I, the low-temperature liquid ammonia storage tank is connected with the outlet of the fourth pipeline 9, the fourth pipeline 9 is provided with two heat source input branches, the heat source outlet of the first low-temperature material preheater and the heat source outlet of the second low-temperature material preheater are respectively connected with the inlets of the two heat source input branches, the second low-temperature material source is connected with the inlet of the fifth pipeline 10, the fifth pipeline 10 is provided with two cold source output branches, the outlets of the two cold source output branches are respectively connected with the cold source inlet of the first low-temperature material preheater and the cold source inlet of the second low-temperature material preheater, the inlet of the second low-temperature material reheater is connected with the sixth pipeline 11, the sixth pipeline 11 is provided with two cold source input branches, the cold source outlet of the first low-temperature material preheater and the cold source outlet of the second low-temperature material preheater are respectively connected with the inlets of the two cold source input branches, the chilled water pipe network is connected with the chilled water storage tank 4 through the chilled water output pipe 12, the chilled water storage tank 4 is connected with a seventh pipeline 13, the seventh pipeline 13 is connected to the heat source inlet of the second low-temperature material preheater through the chilled water circulating pump 5, and the heat source outlet of the second low-temperature material preheater is connected back to the chilled water pipe network through the chilled water circulating pipe 14. And the first pipeline 6, the two heat source output branches and the two cold source output branches are respectively provided with a control valve for controlling the opening and closing of the pipeline and the flow of materials in the pipeline.
According to the structure, the normal-temperature liquid ammonia input from the liquid ammonia source in the process of pouring is cooled through the first low-temperature material in the first low-temperature material source and the second low-temperature material in the second low-temperature material source, and meanwhile, the first low-temperature material and the second low-temperature material which need to be output are preheated through the second low-temperature material preheater, as the purpose of the scheme is to incrementally cool the liquid ammonia pouring and control the temperature of the liquid ammonia at a lower temperature, the cold energy provided by the low-temperature material needs to be ensured, the existing part of the low-temperature material is redundant, namely, the part of the low-temperature material is conveyed to the second low-temperature material preheater, the part does not cool the liquid ammonia, but the output flow and the temperature stability of the low-temperature material which is output through the second low-temperature material preheater need to be ensured, and meanwhile, in order to ensure that the temperature is controllable under the condition that the final output flow of the second low-temperature material is stable, the scheme also stores a certain amount of water through the freezing water storage tank 4, so that the output temperature of the freezing water through the freezing water circulation pump 5 can be controlled to pass through the second low-temperature material preheater is maintained, and the output temperature of the second low-temperature material is regulated. Therefore, the heat exchange station system provided by the scheme can utilize the cold energy of the low-temperature materials to reduce the temperature of liquid ammonia, and because the liquid ammonia is cooled through two low-temperature material sources, the total amount of liquid ammonia pouring is effectively increased, the liquid ammonia temperature input into the low-temperature liquid ammonia storage tank is effectively controlled, meanwhile, the material flow and the temperature stability of the two low-temperature materials output into the corresponding reheater can be effectively ensured, and the cooling of chilled water can be simultaneously realized, so that the cold energy of the low-temperature materials is fully utilized, and the energy consumption of the system is effectively reduced.
In this example, the first low temperature material was low temperature ethylene at-102℃and the second low temperature material was low temperature propane at-42 ℃. The corresponding first low-temperature material source is a low-temperature ethylene storage tank 18 and an ethylene feed pump, the second low-temperature material source is a low-temperature propane storage tank 20 and a propane feed pump, the reheaters are a corresponding ethylene reheater 17 and a corresponding propane reheater 19 respectively, the preheaters are a corresponding ethylene preheater 1, a corresponding propane preheater I2 and a corresponding propane preheater II 3 respectively, and the liquid ammonia source is a liquid ammonia tank car or a liquid ammonia spherical tank and a corresponding liquid ammonia feed pump.
The temperature of the liquid ammonia at normal temperature is 25 ℃, the temperature of chilled water output by a chilled water pipe network is 12 ℃, and the temperature of ethylene input into the ethylene reheater 17 is-53 ℃. Under the stable state, namely under the condition that liquid ammonia and chilled water are stably conveyed and the cold energy of low-temperature materials is fully utilized, the temperature of propane output by the first propane preheater 2 to the propane reheater 19 is-11.6 ℃, the temperature of propane output by the second propane preheater 3 to the propane reheater 19 is-14 ℃, and the temperature of chilled water output by the second propane preheater 3 is 7 ℃; the temperature of the liquid ammonia input into the low-temperature liquid ammonia storage tank by the ethylene preheater 1 is minus 25 ℃, and the temperature of the liquid ammonia input into the low-temperature liquid ammonia storage tank by the propane preheater 1 is minus 6.6 ℃.
As the solidifying point of the liquid ammonia is 77 ℃ below zero and the temperature of ethylene is 102 ℃ below zero, if a single double-tube plate heat exchanger is adopted to directly carry out cold-heat exchange, the liquid ammonia which is retained in the tube bundle cannot be ensured not to freeze when the system is suddenly stopped, ammonia molecules have hydrogen bonds like water molecules, and the volume of the ammonia molecules can be expanded during solidification to cause the tube bundle of the heat exchanger to expand so as to generate a channeling accident. Therefore, the ethylene preheater 1 adopts a dual-composite heat exchanger structure, and comprises an upper composite heat exchanger and a lower composite heat exchanger, wherein the lower composite heat exchanger 15 is provided with a heat source inlet and a heat source outlet of the ethylene preheater 1, normal-temperature liquid ammonia enters a tube side of the lower composite heat exchanger 15 through the heat source inlet, the upper composite heat exchanger 16 is provided with a cold source inlet and a cold source outlet of the ethylene preheater 1, low-temperature ethylene enters the tube side of the upper composite heat exchanger 16 through the cold source inlet, the shell side of the upper composite heat exchanger 16 is communicated with the shell side of the lower composite heat exchanger 15, and heat exchange media are arranged in the two shell sides, and the heat exchange media are propane in the embodiment. In the lower compound heat exchanger 15, propane exchanges heat with liquid ammonia in a tube side, and is heated and gasified by itself to enter a shell side of the upper compound heat exchanger 16, the temperature of the shell side of the lower compound heat exchanger 15 is reduced, and the liquid ammonia is cooled to-25 ℃; in the shell side of the upper compound heat exchanger 16, the gasified propane exchanges heat with low-temperature ethylene, and is condensed, liquefied and reflowed to the shell side of the lower compound heat exchanger 15, and the temperature of the shell side of the upper compound heat exchanger 16 is raised, so that the temperature of ethylene is heated to-53 ℃, and the purposes of reducing the temperature of liquid ammonia and preheating the externally-conveyed ethylene are realized.
After the composite heat exchanger is adopted, the tube side and the shell side are subjected to material channeling, the pressure and liquid level change of the shell side can be effectively monitored, material channeling abnormality can be found early, and the cost is greatly reduced compared with that of an online analyzer. The compound heat exchanger is adopted to ensure that the ethylene and the liquid ammonia do not exchange heat directly, so that the possibility of mutual channeling of two raw materials is basically reduced to zero; the channeling phenomenon in the structure is that the heat exchange medium propane is respectively channeling with the ethylene and the liquid ammonia, and the quality influence on the ethylene and the liquid ammonia is limited because the propane stock in the scheme is only about 3 tons.
In addition to controlling the delivery of each material according to the liquid ammonia pouring demand and the ethylene output demand, the ethylene preheater 1 is also provided with self-controlled interlocking logic as follows:
In order to prevent the low temperature of the shell side propane from causing the liquid ammonia in the tube side of the upper compound heat exchanger 16 to reach freezing point for solidification, an interlocking logic I is arranged, when the temperature of the shell side of the upper compound heat exchanger 16 is lower than-65 ℃, a control valve on the first pipeline 6 and a control valve on a corresponding heat source output pipeline are closed in an interlocking way, the cold source input and the heat source input of the ethylene preheater 1 are cut off, and meanwhile, a direct pipeline is opened to enable low-temperature ethylene to be directly input into the ethylene reheater 17.
In order to prevent pipeline embrittlement accidents caused by the fact that the temperature of the pipeline for outputting liquid ammonia by the lower composite heat exchanger 15 is lower than the design temperature, an interlocking logic II is arranged: when the temperature of the heat source outlet of the lower compound heat exchanger 15 is lower than-40 ℃, the control valve on the first pipeline 6 and the control valve on the corresponding heat source output pipeline are closed in an interlocking way, the cold source input and the heat source input of the ethylene preheater 1 are cut off, and meanwhile, the direct pipeline is opened to enable low-temperature ethylene to be directly input into the ethylene reheater 17.
To prevent the line expansion pressure of the output ethylene of the upper composite heat exchanger 16 from exceeding the design pressure, interlock logic three is provided: when the outlet pressure of the cold source of the upper compound heat exchanger 16 is higher than 2.8Mpa, the control valve on the corresponding heat source output pipeline is closed in an interlocking way, and the heat source input of the ethylene preheater 1 is cut off.
According to the interlocking logic and the position of the propane temperature monitoring point in the shell pass, in order to prevent the interlocking unexpected action when the preheater is put into operation, normal-temperature liquid ammonia is introduced first and then low-temperature ethylene is introduced when the ethylene preheater 1 starts to operate, so that the propane temperature of the heat exchange medium is ensured not to be lower than the interlocking action set value. Before the ethylene preheater 1 is put into service, the ethylene reheater 17 should be ready for heating. After the liquid ammonia at normal temperature is fed into the preheater in a small amount, the low-temperature ethylene is fed into the preheater, and the ethylene reheating output temperature is properly controlled to be no more than-27 ℃ in a short time, so that the low linkage of the outlet temperature of the ethylene reheater 17 is prevented from being triggered. The flow of the normal-temperature liquid ammonia and the low-temperature ethylene into the preheater is firstly regulated, then the steam supply amount of the ethylene reheater 17 is regulated (the reheater reheats the ethylene through steam), and only one technological parameter can be sequentially regulated each time until the output temperature and flow of the ethylene and the liquid ammonia reach stability, thus completing the system application. This avoids the need to adjust the feed rates of two or more media simultaneously, as the presence of two or more variables in the system can cause production fluctuations.
When the propane preheater I2 works, normal-temperature liquid ammonia enters the tube side of the propane preheater I2, and low Wen Bingwan enters the shell side of the propane preheater I2. The preheated propane is input into a propane reheater 19, is further reheated to a production demand temperature by steam heating, and is output. The first propane preheater 2 performs cold-heat exchange to achieve the purposes of reducing the temperature of liquid ammonia and preheating the output propane. The first propane preheater 2 and the second propane preheater 3 have the same structure and are both double-tube plate heat exchangers. Leakage exists between the tube side and the shell side of the tube-plate heat exchanger, and the leakage mainly occurs at the joint of the tube bundle and the tube plate and at the perforation on the tube bundle base material. The double-tube plate type heat exchanger comprises an inner tube plate 22, a tube bundle and an outer tube plate 21, wherein the inner tube plate 22 is sealed with the tube bundle through expansion joint, the outer tube plate 21 is sealed with the tube bundle through welding, a cavity 23 is formed between the inner tube plate 22 and the outer tube plate 21, nitrogen is filled in the cavity 23, the pressure is maintained, a pressure transmitter is arranged, the pressure maintaining pressure is 0.6MPa, and the pressure transmitter is used for monitoring leakage at the joint of the tube bundle and the tube plate. The nitrogen pressure was relatively stable, indicating that a material leak occurred when the pressure in chamber 23 was significantly changed. In order to slow down the tube bundle thinning and perforation caused by the scouring and corrosion of the liquid ammonia to the tube bundle, the wall thickness of the tube bundle is increased to 2.0mm, and the risk of low Wen Bingwan and normal-temperature liquid ammonia channeling is reduced by increasing the corrosion allowance.
For the first propane preheater 2, the low Wen Bingwan (namely, firstly throwing in the shell side) is preferably input so as to prevent the tank pressure from rising rapidly caused by directly feeding normal-temperature liquid ammonia into the low-temperature tank. After the reheating and external delivery of the propane are stable, small amount of normal-temperature liquid ammonia is input into the tube side of the preheater, and then the steam supply amount of the propane reheater 19 is reduced by pressure, and only one technological parameter can be sequentially adjusted at each time; this avoids adjusting the feed of both media, which could cause production fluctuations if two variables were present in the system.
When the propane preheater II 3 works, chilled water from the chilled water circulating pump 5 enters the tube side of the propane preheater I2, and low Wen Bingwan enters the shell side of the propane preheater I2. The low Wen Bingwan is preheated and then sent to the inlet of the propane reheater 19 to be heated to the production demand temperature through steam heating, and the purpose of cooling the chilled water is realized through cold-heat exchange. In this embodiment, the chilled water of the heat exchange station system is initially designed to be pure water to directly exchange heat with low-temperature propane, and the circulating water is extremely easy to freeze, so that the tube bundle is burst to generate an accident. To ensure the safety of the system, chilled water (also called as a cooling medium) is changed into an ethylene glycol aqueous solution with the content of 55 percent (freezing point-45 ℃). However, ethylene glycol is easily oxidized into acidity in air, the pipeline equipment is corrosive, a nitrogen sealing measure is designed for the frozen water tank in order to prevent the ethylene glycol from being oxidized in the frozen water tank, a pressure reducing valve is arranged on a nitrogen supplementing pipeline to maintain constant tank pressure, the pressure of the frozen water tank is prevented from fluctuating along with the change of the environmental temperature, and the air is prevented from entering the frozen water tank through a breather valve. In addition, special corrosion inhibitor is added to the chilled water, so that the corrosiveness of the chilled water is further reduced. In addition, in order to prevent the chilled water pump from evacuating, the system is also provided with self-control interlocking logic: the interlocking stops the chilled water circulation pump 5 when the chilled water level in the chilled water storage tank 4 is below a threshold.
Because the temperature change requirement of the chilled water user in a short time is not harsh, the chilled water user only needs to keep circulating operation, the chilled water is preferably firstly input (namely, a tube side is put into use), after the normal circulating operation of the chilled water, low-temperature propane is slightly input into the shell side of the preheater and gradually extracted, and then the steam supply amount of the propane reheater 19 is reduced until the output temperature of the propane and the chilled water reaches the production requirement. Only one process parameter can be sequentially adjusted at a time, and simultaneously, two variables exist in the system, which can cause production fluctuation. If the chilled water output temperature approaches the lower limit and is in a descending trend, the low Wen Bingwan temperature control valve of the preheater can be adjusted, and the low Wen Bingwan feeding amount of the preheater is reduced to control the chilled water output temperature within the process index range.
While the invention has been described above with reference to the accompanying drawings, it will be apparent that the invention is not limited to the above embodiments, but is capable of being modified or applied to other applications without modification, as long as various insubstantial modifications of the inventive concept and technical solutions are adopted, all within the scope of the invention.
Claims (8)
1. A heat exchange station system for comprehensive utilization of cold energy is characterized in that: comprises a first low-temperature material source, a second low-temperature material source, a liquid ammonia source, a chilled water pipe network, a first low-temperature material reheater, a second low-temperature material reheater, a low Wen Yean storage tank, a first low-temperature material preheater, a second low-temperature material preheater and a chilled water storage tank (4), wherein the first low-temperature material source is connected with a cold source inlet of the first low-temperature material preheater through a first pipeline (6), a cold source outlet of the first low-temperature material preheater is connected with an inlet of the first low-temperature material reheater through a second pipeline (7), the liquid ammonia source is connected with an inlet of a third pipeline (8), the third pipeline (8) is provided with two heat source output branches, outlets of the two heat source output branches are respectively connected with a heat source inlet of the first low-temperature material preheater and a heat source inlet of the second low-temperature material preheater, the low-temperature liquid ammonia storage tank is connected with the outlet of a fourth pipeline (9), the fourth pipeline (9) is provided with two heat source input branches, the heat source outlet of the first low-temperature material preheater and the heat source outlet of the second low-temperature material preheater are respectively connected with the inlets of the two heat source input branches, the second low-temperature material source is connected with the inlet of a fifth pipeline (10), the fifth pipeline (10) is provided with two cold source output branches, the outlets of the two cold source output branches are respectively connected with the cold source inlet of the second low-temperature material preheater and the cold source inlet of the second low-temperature material preheater, the inlet of the second low-temperature material reheater is connected with a sixth pipeline (11), the sixth pipeline (11) is provided with two cold source input branches, the cold source outlet of the first low-temperature material preheater and the cold source outlet of the second low-temperature material preheater are respectively connected to inlets of two cold source input branches, a chilled water pipe network is connected with a chilled water storage tank (4) through a chilled water output pipe (12), the chilled water storage tank (4) is connected with a seventh pipeline (13), the seventh pipeline (13) is connected to a heat source inlet of the second low-temperature material preheater through a chilled water circulating pump (5), and the heat source outlet of the second low-temperature material preheater is connected back to the chilled water pipe network through a chilled water circulating pipe (14).
2. A heat exchange station system for comprehensive utilization of cold energy according to claim 1, wherein: the first low-temperature material is low-temperature ethylene, and the second low-temperature material is low Wen Bingwan; the first low-temperature material source is a low-temperature ethylene storage tank (18) and an ethylene feed pump, the second low-temperature material source is a low-temperature propane storage tank (20) and a propane feed pump, the first low-temperature material reheater is an ethylene reheater (17), the second low-temperature material reheater is a propane reheater (19), the first low-temperature material preheater is an ethylene preheater (1), the second low-temperature material preheater is a propane preheater I (2), the second low-temperature material preheater II is a propane preheater II (3), and the liquid ammonia source is a liquid ammonia tank car or a liquid ammonia spherical tank and a corresponding liquid ammonia feed pump.
3. A heat exchange station system for comprehensive utilization of cold energy according to claim 2, wherein: the ethylene preheater (1) adopts a double composite heat exchanger structure, and comprises an upper composite heat exchanger and a lower composite heat exchanger, wherein the lower composite heat exchanger (15) is provided with a heat source inlet and a heat source outlet of the ethylene preheater (1), normal-temperature liquid ammonia enters a tube pass of the lower composite heat exchanger (15) through the heat source inlet, the upper composite heat exchanger (16) is provided with a cold source inlet and a cold source outlet of the ethylene preheater (1), low-temperature ethylene enters the tube pass of the upper composite heat exchanger (16) through the cold source inlet, the shell passes of the upper composite heat exchanger (16) are communicated with the shell passes of the lower composite heat exchanger (15), heat exchange media are arranged in the two shell passes, and the heat exchange media are propane.
4. A heat exchange station system for integrated utilization of cold energy according to claim 3, wherein: the first propane preheater (2) and the second propane preheater (3) have the same structure and are double-tube plate heat exchangers; the double-tube plate type heat exchanger comprises an inner tube plate (22), a tube bundle and an outer tube plate (21), wherein the inner tube plate (22) is sealed with the tube bundle through expansion joint, the outer tube plate (21) is sealed with the tube bundle through welding, a cavity (23) is formed between the inner tube plate (22) and the outer tube plate (21), nitrogen filling and pressure maintaining are carried out in the cavity (23), a pressure transmitter is arranged, the pressure maintaining pressure is 0.6 MPa, and the pressure transmitter is used for monitoring leakage at the joint of the tube bundle and the tube plate.
5. A heat exchange station system for integrated utilization of cold energy according to claim 4, wherein: and the first pipeline (6), the two heat source output branches and the two cold source output branches are respectively provided with a control valve for controlling the opening and closing of the pipeline and the flow of materials in the pipeline.
6. A heat exchange station system for integrated utilization of cold energy according to claim 5, wherein: the ethylene preheater (1) is also provided with self-controlled interlock logic as follows:
Interlock logic one: when the shell side temperature of the upper composite heat exchanger (16) is lower than-65 ℃, a control valve on the first pipeline (6) and a control valve on a corresponding heat source output pipeline are closed in an interlocking way, the cold source input and the heat source input of the ethylene preheater (1) are cut off, and meanwhile, a direct pipeline is opened to enable low-temperature ethylene to be directly input into the ethylene reheater (17);
And interlocking logic II: when the outlet temperature of the heat source of the lower compound heat exchanger (15) is lower than minus 40 ℃, the control valve on the first pipeline (6) and the control valve on the corresponding heat source output pipeline are closed in an interlocking way, the cold source input and the heat source input of the ethylene preheater (1) are cut off, and meanwhile, the direct pipeline is opened to enable low-temperature ethylene to be directly input into the ethylene reheater (17);
Interlocking logic three: when the outlet pressure of the cold source of the upper compound heat exchanger (16) is higher than 2.8Mpa, the control valve on the corresponding heat source output pipeline is closed in an interlocking way, and the heat source input of the ethylene preheater (1) is cut off.
7. A heat exchange station system for integrated utilization of cold energy according to claim 5, wherein: the system is characterized in that chilled water is glycol water solution with the content of 55%, nitrogen sealing measures are designed for a chilled water storage tank (4), a pressure reducing valve is arranged on a nitrogen supplementing pipeline to maintain the constant tank pressure of the chilled water storage tank (4), and an automatic control interlocking logic is further arranged for preventing a chilled water circulating pump (5) from evacuating: and when the freezing water liquid level in the freezing water storage tank (4) is lower than the threshold value, the freezing water circulation pump (5) is stopped in an interlocking way.
8. A heat exchange station system for integrated utilization of cold energy according to claim 3, wherein: the temperature of the liquid ammonia at normal temperature is 25 ℃, the temperature of chilled water output by a chilled water pipe network is 12 ℃, and the temperature of ethylene input into an ethylene reheater (17) is-53 ℃; in a stable state, the temperature of propane output from the first propane preheater (2) to the propane reheater (19) is-11.6 ℃, the temperature of propane output from the second propane preheater (3) to the propane reheater (19) is-14 ℃, and the temperature of chilled water output from the second propane preheater (3) is 7 ℃; the temperature of the liquid ammonia input into the low-temperature liquid ammonia storage tank by the ethylene preheater (1) is minus 25 ℃, and the temperature of the liquid ammonia input into the low-temperature liquid ammonia storage tank by the propane preheater (2) is minus 6.6 ℃.
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| CN104806311A (en) * | 2015-03-17 | 2015-07-29 | 南京工业大学 | Novel amino thermochemical energy storage system |
| CN107304974A (en) * | 2016-04-25 | 2017-10-31 | 江苏德邦工程有限公司 | Cold energy of liquefied natural gas recovery system and method |
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| JP2014152950A (en) * | 2013-02-05 | 2014-08-25 | Mitsubishi Heavy Ind Ltd | Refrigeration system, ship, and operation method of refrigeration system |
| CN203572091U (en) * | 2013-10-28 | 2014-04-30 | 大连理工大学 | Heating-medium-water-driving ammonia and lithium bromide integrated absorption refrigeration device |
| CN207741617U (en) * | 2017-11-29 | 2018-08-17 | 泰兴金燕化学科技有限公司 | A kind of more cold energy demand utilization systems of ethylene low temperature storing and transporting cold energy fecund line |
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| CN104806311A (en) * | 2015-03-17 | 2015-07-29 | 南京工业大学 | Novel amino thermochemical energy storage system |
| CN107304974A (en) * | 2016-04-25 | 2017-10-31 | 江苏德邦工程有限公司 | Cold energy of liquefied natural gas recovery system and method |
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