CN109553058B - Low-temperature propane ship unloading and heating process - Google Patents
Low-temperature propane ship unloading and heating process Download PDFInfo
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- CN109553058B CN109553058B CN201910015752.8A CN201910015752A CN109553058B CN 109553058 B CN109553058 B CN 109553058B CN 201910015752 A CN201910015752 A CN 201910015752A CN 109553058 B CN109553058 B CN 109553058B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B67—OPENING, CLOSING OR CLEANING BOTTLES, JARS OR SIMILAR CONTAINERS; LIQUID HANDLING
- B67D—DISPENSING, DELIVERING OR TRANSFERRING LIQUIDS, NOT OTHERWISE PROVIDED FOR
- B67D9/00—Apparatus or devices for transferring liquids when loading or unloading ships
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Abstract
The invention provides a device and a process for low-temperature propane ship unloading and heating, which comprise a ship unloading arm, a pre-cooling unit, a pre-cooling buffer unit, a heating and boosting unit and a tank area spherical tank which are sequentially connected, wherein the pre-cooling buffer unit is connected with a condensate recovery unit, and the heating and boosting unit is connected with a heat exchange unit. The invention has the beneficial effects that: the invention designs a whole set of ship unloading and heating device and process including a precooling pipeline, and through a segmented precooling mode, the precooling time of the ship unloading pipeline is effectively shortened, and the stability and the safety of the precooling process are higher; the temperature rise and pressure rise unit for the low-temperature propane is arranged, so that the received low-temperature propane can be raised to-10-0 ℃, the ball tank of the subsequent storage equipment is favorably made of common carbon steel to replace low-temperature steel, and the equipment investment of the ball tank is saved.
Description
Technical Field
The invention belongs to the technical field of low-temperature propane ship unloading processes, and particularly relates to a low-temperature propane ship unloading and heating process.
Background
In the prior art, liquefied propane purchased from overseas ships is unloaded and stored in a tank area storage tank in a land factory, and the tank area storage tank is made of carbon steel generally and can resist the low temperature of minus 19 ℃ at the lowest; however, the temperature of propane in the overseas marine transport ship cabin is about-41 ℃, so a low-temperature propane ship unloading and heating process device is required to be arranged at a wharf, and the low-temperature propane is heated to about 0 ℃ after being safely unloaded and then is conveyed to a storage tank in a tank field for storage. The low temperature ethylene unloading process disclosed in the prior art focuses on the cooling of the unloading pipeline and does not involve the subsequent system of the unloading pipeline. The thawing process of low temperature liquefied hydrocarbon has been also used in some domestic factories, but 20000m is selected3The low-temperature liquefied hydrocarbon storage tank receives low-temperature liquefied hydrocarbon in a cabin, the large-volume storage tank can play a role in storage in a low-temperature ship unloading system, but meanwhile, the pre-cooling of equipment is extremely difficult and dangerous, the temperature of the equipment is required to be reduced by 1 ℃ per hour in the pre-cooling process, the temperature difference between any two points in the storage tank cannot exceed 10 ℃, the temperature reduction time is long, the energy consumption in the pre-cooling process is high, the temperature control difficulty is high, if the structure of the storage tank is slightly imperfect, or the pre-cooling temperature control operation is careless, the low-temperature liquefied hydrocarbon can be caused to fall to the bottom of the storage tank quickly, the storage tank can generate stress due to sudden low temperature,causing large-scale leakage of liquefied hydrocarbons, endangering the safety of tank farms and surrounding personnel, and making improvements urgently needed.
Disclosure of Invention
In order to solve the technical problems, the invention solves the problem of unloading the low-temperature propane in the ship to the spherical tank in the land tank area by researching and developing a novel low-temperature propane unloading and heating device and process.
In order to solve the technical problems, the invention adopts the technical scheme that:
a low-temperature propane ship unloading and warming device comprises a ship unloading arm, a pre-cooling unit, a pre-cooling buffer unit, a warming and boosting unit and a tank area spherical tank which are sequentially connected, wherein the pre-cooling buffer unit is connected with a condensate recovery unit, and the warming and boosting unit is connected with a heat exchange unit;
the pre-cooling unit comprises a plurality of pre-cooling pipelines for pre-cooling the ship unloading pipeline, the pre-cooling buffer unit comprises a propane buffer tank, the temperature and pressure raising unit comprises a propane delivery pump, a propane heater and a low-temperature propane bypass, and the ship unloading arm, the ship unloading pipeline, a liquid path outlet of the propane buffer tank, the propane delivery pump, the propane heater and the tank area spherical tank are sequentially connected.
Further, the propane buffer tank is 100m3The stainless steel pressure storage tank.
Furthermore, a plurality of sections of precooling pipelines are arranged in parallel, the plurality of sections of precooling pipelines are communicated with the tank field spherical tank, and the plurality of sections of precooling pipelines are communicated with the tank wagon through quick connectors.
Further, the condensate recovery unit comprises a compressor, a condenser and a propane recovery tank which are connected in sequence, the gas path outlet of the propane buffer tank is communicated with the compressor, the condenser and the propane recovery tank in sequence, and the propane recovery tank is communicated with the tank area spherical tank.
Further, the heat exchange unit comprises an ethylene glycol aqueous solution storage tank, an ethylene glycol circulating pump and a steam heat exchanger which are connected in sequence, the ethylene glycol aqueous solution storage tank is communicated with an ethylene glycol aqueous solution outlet of the propane heater, and the steam heat exchanger is communicated with an ethylene glycol aqueous solution inlet of the propane heater.
In addition, the invention also discloses a low-temperature propane ship unloading and heating process, which comprises the following main steps:
(1) pre-cooling an unloading pipeline and a propane buffer tank:
the precooling process is divided into two working conditions, under the working condition of first start-up, precooled propane liquid from a tank car enters an unloading pipeline after passing through a plurality of sections of precooling pipelines and finally enters a propane buffer tank; under the working condition of subsequent start-up, precooled propane liquid from the spherical tank of the tank area enters an unloading pipeline after passing through a plurality of sections of precooling pipelines and finally enters a propane buffer tank; after precooling to a preset temperature, the ship unloading arm starts unloading, and low-temperature propane enters a propane buffer tank through a ship unloading pipeline;
(2) post-treatment of pre-cooled propane liquid:
precooling propane liquid entering a ship unloading pipeline is decompressed, then is subjected to flash evaporation and heat absorption to be changed into a gas-liquid two phase, propane gas entering a propane buffer tank enters a tank area spherical tank through a compressor, a condenser and a propane recovery tank, propane liquid at the bottom in the propane buffer tank is used for precooling a propane delivery pump and a pipeline behind the pump, and precooled propane gas returns to the propane buffer tank through a pipeline;
(3) preheating a propane heater:
heating medium ethylene glycol aqueous solution in the propane heater sequentially enters an ethylene glycol aqueous solution storage tank, an ethylene glycol circulating pump and a steam heat exchanger and then enters the propane heater, low-temperature propane in a propane buffer tank enters the propane heater through a propane delivery pump and exchanges heat with the ethylene glycol aqueous solution, and the ethylene glycol aqueous solution after heat exchange is recycled to the ethylene glycol aqueous solution storage tank;
(4) and (3) boosting and heating low-temperature propane:
the low-temperature propane enters a propane heater to be heated to-10-0 ℃ and then is sent to a spherical tank in the tank area;
when the heated propane liquid is higher than 0 ℃, opening a large and low temperature propane bypass regulating valve, and finely adjusting the temperature of the propane fed into the spherical tank in the tank area; when the temperature of the heated propane liquid is lower than-10 ℃, the DCS system alarms when the temperature is low, and manual intervention is carried out; when the temperature of the heated propane liquid is lower than-16 ℃, the DCS alarms when the temperature is low, locks the propane delivery pump in parallel, transmits a pump stopping signal of the propane delivery pump to the wharf control room, stops unloading the ship arm and stops unloading.
Further, in the precooling process in the step (1), the cooling rate of the ship unloading pipeline and the propane buffer tank is 5-8 ℃/h.
Further, in the precooling process in the step (1), precooling is carried out on precooled propane liquid entering an unloading pipeline through decompression of 0.025-0.1 MPaG, and the flow rate of the precooling propane liquid is 800-1200 kg/h.
Further, the concentration of the ethylene glycol aqueous solution in the above step (3) is 60% by weight.
The low-temperature propane ship unloading and heating process has the following advantages:
(1) the invention designs a whole set of ship unloading and heating device and process including a precooling pipeline, effectively shortens the precooling time of the ship unloading pipeline by a segmented precooling mode, and has higher stability and safety in the precooling process; the temperature rise and pressure rise unit for the low-temperature propane is arranged, so that the received low-temperature propane can be raised to-10-0 ℃, the ball tank of the subsequent storage equipment is favorably made of common carbon steel to replace low-temperature steel, and the equipment investment of the ball tank is saved;
(2) the process flow of the invention adopts 100m3The stainless steel pressure storage tank is used as a buffer tank for the ship unloading low-temperature propane medium, and can solve the problems that a large normal-pressure storage tank is difficult to pre-cool and has long pre-cooling time;
(3) the method is used for precooling the ship unloading pipeline, and precooling is carried out by adopting a mode of connecting a tank car with a quick coupling on the precooling pipeline when the ship unloading pipeline is started for precooling for the first time; then precooling operation is carried out to lead propane liquid from a propane spherical tank in the tank area, and precooling ship unloading pipelines are circulated in a way that pressure is reduced by a pressure reducing valve to ensure that part of the liquid is vaporized and absorbs heat;
(4) the invention not only precools the ship unloading pipeline, but also precools the propane buffer tank of the subsequent process of the ship unloading pipeline, and precools the propane delivery pump and the pipeline behind the pump by using the propane liquid in the precooling process of the propane buffer tank, thereby ensuring the safety of the low-temperature propane caching and delivery process;
(5) the mixed solution of the ethylene glycol and the water with mild heat exchange is used as a heat source for heating the low-temperature propane, so that the phenomenon that the low-temperature propane is subjected to temperature runaway vaporization due to overhigh temperature of the heat source in the heat exchange process, and the overpressure release of propane heat exchanger equipment is caused is avoided;
(6) in the propane heating process flow, a low-temperature propane bypass pipeline is arranged for a propane heater, the temperature of a propane medium conveyed to a tank area after heating can be effectively regulated and controlled, the regulation is carried out according to the temperature range which can be borne by a subsequent propane spherical tank, the consumption of a heat source can be reduced to the greatest extent, and the production cost is saved.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate an embodiment of the invention and, together with the description, serve to explain the invention and not to limit the invention. In the drawings:
FIG. 1 is a process flow diagram of the present invention;
FIG. 2 is a process diagram of the present invention;
fig. 3-5 are enlarged schematic views of various portions of fig. 1 to illustrate the valve and meter numbers therein.
Wherein: the system comprises an A-precooling unit, an A1-ship unloading pipeline, an A2-first-section precooling pipeline, an A3-second-section precooling pipeline, an A4-quick joint, a B-precooling buffer unit, a B1-propane buffer tank, a C-temperature and pressure raising unit, a C1-propane delivery pump, a C2-propane heater, a C3-low-temperature propane bypass, a D-condensate recovery unit, a D1-compressor, a D2-condenser, a D3-propane recovery tank, an E-heat exchange unit, an E1-ethylene glycol aqueous solution storage tank, an E2-ethylene glycol circulating pump and an E3-steam heat exchanger.
Detailed Description
It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like, indicate orientations or positional relationships based on those shown in the drawings, and are used only for convenience in describing the present invention and for simplicity in description, and do not indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and thus, are not to be construed as limiting the present invention. Furthermore, the terms "first", "second", etc. are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first," "second," etc. may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless otherwise specified.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art through specific situations.
The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings.
In some embodiments, the length of the ship unloading pipeline is about 2000m, during the ship unloading process, if low-temperature propane directly enters the ship unloading pipeline, the temperature change is large in a short time, the pipeline material or the flange connection part is damaged due to excessive thermal stress, and propane leakage is caused. A two-section segmented precooling mode is adopted during precooling, namely two sections of precooling pipelines are arranged to precool the ship unloading pipeline, the two sections of precooling pipelines are respectively a first section of precooling pipeline and a second section of precooling pipeline, the first section of precooling pipeline and a precooling valve XV-1114 are arranged at the side close to the tank area, and the second section of precooling pipeline and a precooling valve EV-1113 are arranged at the side close to the wharf; during precooling, the pipeline is cooled by injecting precooling media into two sections of precooling pipelines simultaneously, the cooling speed is monitored by thermometers TE-1101, TG-1102, TG-1104 and TE-1105, the speed is strictly controlled to be 5-8 ℃ per hour, and the pipeline is precooled to the temperature of-28 to-36 ℃, so that the pipeline or a propane buffer tank is prevented from being quenched due to too fast cooling. The precooling time can be greatly shortened by adopting a mode that one section of precooling pipeline is respectively arranged at the wharf and the tank area and two sections of cooling pipelines are simultaneously cooled.
The propane liquid used for precooling under the first start working condition is from a tank car, the propane liquid used for precooling under the subsequent start working condition is from a spherical tank in a tank area, the flow is controlled to be 800-1200 kg/h through a flow meter FT-1214 and an adjusting valve FV-1214, and the precooled propane liquid enters an unloading pipeline for precooling after the pressure is reduced to 0.025-0.1 MPaG. The precooling pipeline is provided with pressure indication and temperature indication, online monitoring is carried out, and a safety valve is arranged as an overpressure protection measure. Propane liquid from a precooling pipeline is decompressed by FV-1214, is subjected to flash evaporation and heat absorption to be changed into gas-liquid two phases, enters a propane buffer tank through an unloading pipeline and continues to precool a tank body, and propane gas enters a compressor, a condenser and a propane recovery tank through a gas path outlet at the top of the buffer tank and then enters a tank area spherical tank for storage, wherein the pressure of the propane gas at the outlet of the compressor is 1.9 MPaG; the propane liquid at the bottom of the buffer tank can be used for precooling a propane delivery pump and a pipeline behind the pump, and precooled propane gas returns to the propane buffer tank through a pipeline where FV-1217 is located.
In some embodiments, the propane surge tank is a cryogenic pressurized vertical tank with a normal operating pressure of about 0.15MPaG and a design pressure of 1.77 MPaG. The following factors are mainly responsible for the rise in the pressure of the propane buffer tank: (1) feeding; (2) the storage tank and propane temperature rise; (3) regulator valve PV-1207B fails open. The pressure reduction of the propane buffer tank is mainly caused by the following factors: (1) the propane compressor is not stopped in time; (2) the discharging speed is too high; (3) the propane buffer tank regulating valve PV-1207B is closed due to fault.
When the pressure of the propane buffer tank rises to 0.2MPaG, the propane compressor is started; when the pressure of the propane buffer tank is continuously increased to 0.3MPaG, a regulating valve PV-1207A leading to a plant flare system is started to be opened; when the pressure reaches 0.4MPaG, the regulating valve PV-1207A is fully opened; when the pressure drops to 0.2MPaG, the PV-1207A valve is fully closed. When the pressure of the buffer tank is reduced to 50KPaG, the regulating valve PV-1207B is started; when the pressure in the storage tank is lower than 15KPaG, the valve PV-1207B is fully opened; when the pressure rises to 150KPaG, the valve is fully closed. When the PV-1207B valve is fully opened and the pressure of the storage tank still shows a continuous descending trend, the nitrogen pipeline switch valve XV-1237 is opened to supply nitrogen until the XV-1237 is closed when the pressure reaches a normal value.
In some embodiments, in order to reduce the cost of the propane spherical tank equipment in the tank area, the propane spherical tank is made of carbon steel, the temperature of the propane spherical tank is as low as minus 19 ℃, and the low-temperature propane which is unloaded needs to be heated to above minus 19 ℃ and can be conveyed to the storage tank for storage. Sending low-temperature (about-41 ℃) propane sent from the wharf to the temperature and pressure increasing link, and pressurizing to 1.7-1.9 MPaG through a propane delivery pump; the pressurized low-temperature propane liquid enters a propane heater, exchanges heat with ethylene glycol aqueous solution, and then is sent to a propane tank area after the temperature is raised to-10-0 ℃. Before entering the propane heater, a low temperature propane bypass line is provided, through which regulator valve TV-1224 on the heater outlet regulates the propane liquid temperature between-10 deg.C and 0 deg.C, which temperature range is monitored by remote thermometer TE-1242. When the temperature of the heated propane liquid is lower than-10 ℃, the DCS system alarms when the temperature is low, and manual intervention is carried out; when the temperature is lower than-16 ℃, the DCS system stops the propane delivery pump in an interlocking manner when the temperature is low, then transmits a pump stopping signal of the propane delivery pump to the wharf control room, stops unloading the ship arm and stops unloading.
In some embodiments, a glycol aqueous solution with a concentration of 60% wt is filled in a glycol aqueous solution storage tank (the freezing point of the glycol aqueous solution with the concentration of 60% wt is-50 ℃), heat exchange is carried out between the glycol aqueous solution and low-temperature propane of a propane heater, the cooled glycol aqueous solution returns to the glycol aqueous solution storage tank, the glycol aqueous solution is pressurized by a glycol circulating pump in a glycol heat exchange unit, and then heat is absorbed through heat exchange with steam and circulated to the propane heater again for heat exchange. The method utilizes the glycol aqueous solution with a lower freezing point to exchange heat with the low-temperature propane, and does not adopt a mode of directly heating by steam, because the heat exchange temperature of the glycol aqueous solution is controllable, the heat exchange process is mild, the temperature of saturated steam is higher than that of the low-temperature propane, the heat exchange temperature is low in controllability during direct heating, the regulation is not easy, and the low-temperature propane is easy to fly and vaporize, so that the overpressure of propane heat exchanger equipment is caused, the safety valve jumps, and the material leaks.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and should not be taken as limiting the invention, so that any modifications, equivalents, improvements and the like, which are within the spirit and principle of the present invention, should be included in the scope of the present invention.
Claims (4)
1. A low-temperature propane ship unloading and heating process is characterized by comprising the following main steps:
(1) pre-cooling an unloading pipeline and a propane buffer tank:
the precooling process is divided into two working conditions, under the working condition of first start-up, precooled propane liquid from a tank car enters an unloading pipeline after passing through a plurality of sections of precooling pipelines and finally enters a propane buffer tank; under the working condition of subsequent start-up, precooled propane liquid from the spherical tank of the tank area enters an unloading pipeline after passing through a plurality of sections of precooling pipelines and finally enters a propane buffer tank; after precooling to a preset temperature, the ship unloading arm starts unloading, and low-temperature propane enters a propane buffer tank through a ship unloading pipeline;
(2) post-treatment of pre-cooled propane liquid:
precooling propane liquid entering a ship unloading pipeline is decompressed, then is subjected to flash evaporation and heat absorption to be changed into a gas-liquid two phase, propane gas entering a propane buffer tank enters a tank area spherical tank through a compressor, a condenser and a propane recovery tank, propane liquid at the bottom in the propane buffer tank is used for precooling a propane delivery pump and a pipeline behind the pump, and precooled propane gas returns to the propane buffer tank through a pipeline;
(3) preheating a propane heater:
heating medium ethylene glycol aqueous solution in the propane heater sequentially enters an ethylene glycol aqueous solution storage tank, an ethylene glycol circulating pump and a steam heat exchanger and then enters the propane heater, low-temperature propane in a propane buffer tank enters the propane heater through a propane delivery pump and exchanges heat with the ethylene glycol aqueous solution, and the ethylene glycol aqueous solution after heat exchange is recycled to the ethylene glycol aqueous solution storage tank;
(4) and (3) boosting and heating low-temperature propane:
the low-temperature propane enters a propane heater to be heated to-10-0 ℃ and then is sent to a spherical tank in the tank area;
when the heated propane liquid is higher than 0 ℃, opening a large and low temperature propane bypass regulating valve, and finely adjusting the temperature of the propane fed into the spherical tank in the tank area; when the temperature of the heated propane liquid is lower than-10 ℃, the DCS system alarms when the temperature is low, and manual intervention is carried out; when the temperature of the heated propane liquid is lower than-16 ℃, the DCS alarms when the temperature is low, locks the propane delivery pump in parallel, transmits a pump stopping signal of the propane delivery pump to the wharf control room, stops unloading the ship arm and stops unloading.
2. The low-temperature propane ship unloading and heating process as claimed in claim 1, wherein in the pre-cooling process in the step (1), the cooling rate of the ship unloading pipeline and the propane buffer tank is 5-8 ℃/h.
3. The low-temperature propane ship unloading and heating process according to claim 1, wherein in the precooling process in the step (1), precooling is performed on precooled propane liquid entering a ship unloading pipeline after the pressure reduction is 0.025-0.1 MPaG, and the flow rate of the precooled propane liquid is 800-1200 kg/h.
4. A low temperature propane ship unloading and heating process as claimed in claim 1, wherein the concentration of the ethylene glycol aqueous solution in step (3) is 60% wt.
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