CN114699788A - Oil tanker dock oil gas recovery method - Google Patents
Oil tanker dock oil gas recovery method Download PDFInfo
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- CN114699788A CN114699788A CN202210261673.7A CN202210261673A CN114699788A CN 114699788 A CN114699788 A CN 114699788A CN 202210261673 A CN202210261673 A CN 202210261673A CN 114699788 A CN114699788 A CN 114699788A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0051—Regulation processes; Control systems, e.g. valves
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0036—Multiple-effect condensation; Fractional condensation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0039—Recuperation of heat, e.g. use of heat pump(s), compression
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
- C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
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- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
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Abstract
The invention discloses an oil and gas recovery method for an oil tanker dock, which comprises the following steps: the oil gas to be treated sent in from the oil gas inlet is sent into an oil gas system, sequentially passes through a regenerative heat exchanger, a precooling heat exchanger, a shallow cooling heat exchanger, a deep cooling heat exchanger and a gas fluorine heat exchanger in the oil gas system, is liquefied by exchanging heat with a refrigerant sent out by a refrigeration system, is sent into the regenerative heat exchanger again after being treated by the gas fluorine heat exchanger, and is discharged after exchanging heat in the regenerative heat exchanger; when the system needs defrosting, the high-temperature high-pressure refrigerant is sent into the shallow cooling heat exchanger and the deep cooling heat exchanger for defrosting. The invention not only ensures the temperature fluctuation of the cold field of the oil gas recovery device at the oil tanker dock to be +/-4 ℃, but also improves the energy efficiency by more than 40 percent.
Description
Technical Field
The invention belongs to the technical field of oil gas recovery, and particularly relates to an oil gas recovery method for an oil tanker dock.
Background
The construction and the start of the oil gas recovery facility at the wharf are late, and the actual operation experience is insufficient. And then, the oil gas recovery of the crude oil wharf is steadily promoted along the sea, more and more oil gas recovery facilities are installed in the wharf, the continuous operation of the oil gas recovery facilities of the wharf can basically meet the continuity of ship loading, but the use effects are different, and the energy consumption is higher. In the prior art, for example, a wharf oil gas recovery device (CN2013104309861), the problem of continuous operation of the device is solved, but for chemical VOCs waste gas, no standby cold field exists due to deep cooling, and the wharf 24h continuous operation cannot be realized. And the oil gas temperature fluctuation of the existing oil gas recovery facilities of the oil-gas terminal is large and the energy consumption of the unit is large.
Disclosure of Invention
The purpose of the invention is as follows: in order to solve the problems in the prior art, the invention provides an oil and gas recovery method for an oil tanker dock, which can realize continuous oil and gas recovery and has small oil and gas temperature fluctuation and low energy consumption.
The technical scheme is as follows: the oil and gas recovery method for the oil tanker dock comprises the following steps:
(S1) sending the oil gas to be processed, which is sent from the oil gas inlet, into the oil gas system, sequentially passing through a regenerative heat exchanger, a precooling heat exchanger, a shallow cooling heat exchanger, a deep cooling heat exchanger and a gas fluorine heat exchanger in the oil gas system, liquefying the oil gas by exchanging heat with a refrigerant sent out by a refrigeration system, sending the oil gas processed by the gas fluorine heat exchanger into the regenerative heat exchanger again, and discharging the oil gas after exchanging heat in the regenerative heat exchanger;
(S2) the refrigeration system includes a primary refrigeration system, a secondary refrigeration system, and a tertiary refrigeration system; the primary refrigeration system respectively sends the refrigerant into the precooling heat exchanger and the shallow cooling heat exchanger to exchange heat with oil gas; the secondary refrigeration system sends the refrigerant into a gas-fluorine heat exchanger to exchange heat with oil gas, and the refrigerant after heat exchange is sent into an evaporative condenser; the three-stage refrigeration system sends the refrigerant into the cryogenic heat exchanger to exchange heat with the oil gas, and the refrigerant after heat exchange returns to a refrigeration compressor of the three-stage refrigeration system to carry out refrigeration cycle;
(S3) when the system needs defrosting, the high-temperature high-pressure refrigerant sent from the first-stage refrigeration system is sent to the shallow cooling heat exchanger for defrosting, and the high-temperature high-pressure refrigerant sent from the third-stage refrigeration system is sent to the deep cooling heat exchanger for defrosting.
As a preferred embodiment of the present invention, the shallow cold heat exchanger comprises a first shallow cold heat exchanger and a second shallow cold heat exchanger arranged in parallel; the cryogenic heat exchanger comprises a first cryogenic heat exchanger and a second cryogenic heat exchanger which are arranged in parallel.
The oil-gas system comprises an air pump communicated with an oil-gas inlet, a regenerative heat exchanger connected with the air pump, a precooling heat exchanger connected with a hot-side gas path outlet of the regenerative heat exchanger, a first shallow cooling heat exchanger and a second shallow cooling heat exchanger which are respectively connected with a gas path outlet of the precooling heat exchanger, a first cryogenic heat exchanger connected with a gas path outlet of the first shallow cooling heat exchanger, a second cryogenic heat exchanger connected with a gas path outlet of the second shallow cooling heat exchanger, a gas-liquid separation tank respectively connected with outlets of the first cryogenic heat exchanger and the second cryogenic heat exchanger, a gas-fluorine heat exchanger connected with a gas path outlet of the gas-liquid separation tank, and a regenerative heat exchanger connected with a gas path outlet of the gas-fluorine heat exchanger.
As a preferred embodiment of the present invention, the primary refrigeration system includes a primary refrigeration compressor and a primary condenser connected to a refrigerant outlet of the primary refrigeration compressor, and an outlet of the primary condenser is connected to inlets of the pre-cooling heat exchanger, the first shallow cooling heat exchanger, and the second shallow cooling heat exchanger, respectively; the secondary refrigeration system comprises a secondary refrigeration compressor, a secondary condenser and an evaporative condenser, wherein the secondary condenser is connected with the outlet of the secondary refrigeration compressor; an outlet of the secondary condenser is connected with a refrigerant inlet of the gas-fluorine heat exchanger, and an evaporation side inlet of the evaporative condenser is connected with an outlet of the gas-fluorine heat exchanger; the three-stage refrigeration system comprises a three-stage refrigeration compressor and an evaporative condenser connected with the three-stage refrigeration compressor; and the outlet of the condensation side of the evaporative condenser is respectively connected with the inlets of the first cryogenic heat exchanger and the second cryogenic heat exchanger.
As a preferred embodiment of the present invention, two defrosting branches are respectively led out from an outlet of the primary compressor and connected with the first shallow cooling heat exchanger and the second shallow cooling heat exchanger; and a condensation side inlet of the evaporative condenser is respectively led out two defrosting branches to be connected with the first cryogenic heat exchanger and the second cryogenic heat exchanger.
As a preferred embodiment of the invention, the refrigerant sent by the two defrosting branches led out from the outlet of the primary compressor is merged with the refrigerant sent by the outlet of the primary condenser; and two defrosting branches led out from the condensation side inlet of the evaporative condenser are used for converging the refrigerant after heat exchange with the refrigerant sent into the evaporative condenser again.
As a preferred embodiment of the present invention, a switching control valve is disposed between inlets of the two defrosting branches led out from the condensing side of the evaporative condenser and outlets of the two defrosting branches.
As a preferred embodiment of the present invention, an inlet of the pre-cooling heat exchanger is provided with a pre-cooling throttling element, an inlet of the first shallow cooling heat exchanger is provided with a first throttling element, and an inlet of the second shallow cooling heat exchanger is provided with a second throttling element; a third throttling element is arranged between the outlet of the condensation side of the evaporative condenser and the inlet of the first cryogenic heat exchanger, and a fourth throttling element is arranged between the outlet of the condensation side of the evaporative condenser and the inlet of the second cryogenic heat exchanger; and/or a fifth throttling element is arranged between the outlet of the gas-fluorine heat exchanger and the evaporation side inlet of the evaporative condenser.
As a preferred embodiment of the present invention, a first control valve is disposed between the outlet of the primary compressor and the first shallow cooling heat exchanger, and a second control valve is disposed between the outlet of the primary compressor and the second shallow cooling heat exchanger; the outlets of the first shallow cooling heat exchanger and the second shallow cooling heat exchanger are respectively provided with a third control valve and a fourth control valve; a fifth control valve is arranged between the condensation side inlet of the evaporative condenser and the first cryogenic heat exchanger, and a sixth control valve is arranged between the condensation side inlet of the evaporative condenser and the second cryogenic heat exchanger; and the outlets of the first cryogenic heat exchanger and the second cryogenic heat exchanger are respectively provided with a seventh control valve and an eighth control valve.
As a preferred embodiment of the present invention, the oil gas system is further provided with a control system, and the control system includes a pressure transmitter and a shut-off valve, which are arranged between the oil gas inlet and the air pump. The control system also comprises a first differential pressure transmitter, a second differential pressure transmitter, a three-way reversing valve of a control loop and a control element, wherein the control element is preferably a PLC control module and integrates Siemens control software or GE (GE) and other control software.
In a preferred embodiment of the present invention, the first to eighth control valves are pneumatically double-acting low-temperature shut-off valves.
The low-temperature switching valve comprises a valve body, a valve seat arranged in the valve body, a valve core element connected with the valve seat, a push rod fixed with the upper end of the valve core element and an air cylinder arranged at the top end of the push rod, wherein a valve cavity is formed in the periphery of the valve core element; the valve core element comprises a connecting rod, a corrugated pipe section arranged on the periphery of the connecting rod, a valve core arranged at the lower end of the corrugated pipe section, and a sealing plate arranged at the upper end of the corrugated pipe section, wherein the sealing plate and the connecting rod are sealed.
As a preferred embodiment of the present invention, the air cylinder includes a cylinder liner, an upper cylinder cover and a lower cylinder cover which are disposed at upper and lower ends of the cylinder liner, a first air source interface disposed on the upper cylinder cover, a second air source interface disposed on the lower cylinder cover, and a piston disposed in the cylinder liner, and a bottom end of the piston is connected to the push rod; and/or the valve body and the valve cavity are fixed through a first bolt.
In a preferred embodiment of the present invention, the bellows segment includes a connection section, a fixed plate, and a bellows section disposed between the valve element and the fixed plate.
In a preferred embodiment of the present invention, the valve seat is fixed to the valve element by a second bolt.
In a preferred embodiment of the present invention, a valve chamber gasket is disposed between the valve body and the valve core member.
In a preferred embodiment of the present invention, the valve cavity gasket material is polytetrafluoroethylene.
As a preferred embodiment of the present invention, a first connecting flange is disposed at a top end of the valve chamber, and the first connecting flange is fixed to the lower cylinder cover through a first upright post.
As a preferred embodiment of the present invention, a dust ring, a packing and an O-ring are disposed between the top of the valve cavity and the push rod.
As a preferred embodiment of the present invention, the top of the valve chamber and the bottom end of the push rod are fixed by a first nut.
In a preferred embodiment of the present invention, a piston ring is provided between the piston and the inner wall of the cylinder.
In a preferred embodiment of the present invention, the upper cylinder head and the lower cylinder head are fixed to each other by a second bolt.
As a preferred embodiment of the present invention, a first differential pressure transmitter is disposed between the first shallow cooling heat exchanger and the first cryogenic heat exchanger; and a second differential pressure transmitter is arranged between the second shallow cooling heat exchanger and the second deep cooling heat exchanger.
Preferably, the regenerative heat exchanger is a 30 ℃ cold field heat exchanger, and has no ice blockage hidden danger; the pre-cooling heat exchanger is a 4 ℃ (adjustable) cold field heat exchanger, and has no ice blockage hidden danger; the first shallow cooling heat exchanger A and the second shallow cooling heat exchanger B are cold field heat exchangers with the temperature of minus 25 ℃ (adjustable); the first cryogenic heat exchanger and the second cryogenic heat exchanger are cold field heat exchangers with the temperature of 70 ℃ below zero (adjustable).
Has the advantages that: (1) according to the invention, different heat exchangers are arranged, so that the heat exchangers are ensured to have no ice blockage risk in normal work in the oil gas recovery treatment process, and the regenerative heat exchanger regenerates heat by using temperature difference and does not frost; controlling the temperature of the precooling heat exchanger to be higher than the dew point temperature of the oil gas, so that frosting is avoided; the gas-fluorine heat exchanger utilizes the cold energy of low-temperature oil gas to supercool the refrigerant, the high-temperature refrigerant is moved by a tube pass, the oil gas is in a temperature rise process and cannot frost, and the cold energy of the oil gas is absorbed by the refrigerant of the second refrigeration system and is used for supercooling to improve the refrigeration energy efficiency; (2) the invention sets a shallow cooling heat exchanger and a deep cooling heat exchanger with ice blockage hidden danger into two, an oil gas system is divided into two paths, namely a path A and a path B, one path is normally operated and the other path is standby, so that the continuous operation of the whole device can be ensured; the requirement of continuous operation of oil and gas recovery facilities of an oil tanker wharf is met; (3) differential pressure transmitters are further respectively arranged between the shallow cooling heat exchangers and the deep cooling heat exchangers of the channel A and the channel B, the differential pressure value and the running time of an oil-gas channel are measured, and a proper oil-gas channel is selected to ensure the continuity of the device; (4) the temperature fluctuation in the oil gas recovery process is small, and the throttling element is an electronic expansion valve which can accurately adjust the flow of the refrigerant and effectively stabilize the oil gas temperature of each stage of cold field; secondly, the control valve adopts a zero-leakage pneumatic double-acting piston low-temperature cut-off valve with multiple sealing protection, so that the external leakage of the refrigerant is avoided, the internal leakage of the refrigerant is avoided, and the temperature fluctuation is maintained; finally, when the channel is switched, the device precools the standby oil-gas channel in advance through the control system, and when the standby channel reaches the set temperature, the switching is carried out, so that the temperature fluctuation can be controlled to be +/-4 ℃ in the switching process. (6) The oil gas recovery of the invention has low energy consumption: the energy recovery device is provided with a regenerative heat exchanger for primary energy recovery, a gas-fluorine heat exchanger for reducing the supercooling degree of a refrigerant and improving the energy efficiency of the refrigeration compressor, and oil-cooling recoverers are arranged at the bottoms of the precooling heat exchanger, the shallow cooling heat exchanger and the deep cooling heat exchanger for improving the energy efficiency of the refrigeration compressor; (7) the invention controls the double-path cold field system through the single compressor, and at least reduces the energy consumption of the unit by 40 percent.
Drawings
Fig. 1 is a schematic view of an oil and gas system of an oil and gas recovery device of an oil tanker terminal of the present invention;
fig. 2 is a schematic diagram of a primary refrigeration system of the oil tanker dock oil gas recovery device of the present invention;
fig. 3 is a schematic diagram of the two-stage refrigeration and three-stage refrigeration system of the oil recovery device of the oil tanker dock of the present invention;
FIG. 4 is an exploded view of the low temperature switching valve of the present invention;
fig. 5 is a sectional view of a spool member in the low temperature switching valve of the present invention;
fig. 6 is a sectional view of the low temperature switching valve of the present invention.
Detailed Description
Example 1: as shown in fig. 1-3, the oil tanker dock oil and gas recovery method of the present invention comprises the following steps:
(S1) sending the oil gas to be processed, which is sent from the oil gas inlet, into the oil gas system, sequentially passing through a regenerative heat exchanger, a precooling heat exchanger, a shallow cooling heat exchanger, a deep cooling heat exchanger and a gas fluorine heat exchanger in the oil gas system, liquefying the oil gas by exchanging heat with a refrigerant sent out by a refrigeration system, sending the oil gas processed by the gas fluorine heat exchanger into the regenerative heat exchanger again, and discharging the oil gas after exchanging heat in the regenerative heat exchanger;
(S2) the refrigeration system includes a primary refrigeration system, a secondary refrigeration system, and a tertiary refrigeration system; the primary refrigeration system respectively sends the refrigerant into the precooling heat exchanger and the shallow cooling heat exchanger to exchange heat with oil gas; the secondary refrigeration system sends the refrigerant into a gas-fluorine heat exchanger to exchange heat with oil gas, and the refrigerant after heat exchange is sent into an evaporative condenser; the three-stage refrigeration system sends the refrigerant into a cryogenic heat exchanger to exchange heat with oil gas, and the refrigerant after heat exchange is sent to a refrigeration compressor of the three-stage refrigeration system to carry out refrigerant circulation;
(S3) when the system needs defrosting, the high-temperature high-pressure refrigerant sent from the first-stage refrigeration system is sent to the shallow cooling heat exchanger for defrosting, and the high-temperature high-pressure refrigerant sent from the third-stage refrigeration system is sent to the deep cooling heat exchanger for defrosting.
Specifically, the oil and gas system comprises a first flame arrester 101, a condensate tank 102, an air pump 103, a second flame arrester 104, a regenerative heat exchanger 105, a precooling heat exchanger 106, a first shallow cooling heat exchanger 107, a second shallow cooling heat exchanger 108, a first cryogenic heat exchanger 109, a second cryogenic heat exchanger 110, a gas-liquid separation tank 111 and a gas-fluorine heat exchanger 112. The import of condensate tank 102 links to each other with the oil gas import, the export of condensate tank 102 links to each other with air pump 103's import, air pump 103's export links to each other with the hot side gas circuit import of backheating heat exchanger 105, be provided with first spark arrester 101 between condensate tank 102's import and the oil gas import, be provided with second spark arrester 104 between air pump 103's export and the hot side gas circuit import of backheating heat exchanger 105, in this embodiment, air pump 103 is explosion-proof frequency conversion roots air pump, first spark arrester 101 is explosion-proof type spark arrester, second spark arrester 104 is explosion-proof type spark arrester.
Oil gas is sent into a regenerative heat exchanger 105 under the action of an air pump 103, a hot side gas path outlet of the regenerative heat exchanger 105 is connected with an inlet of a precooling heat exchanger 106, a gas path outlet of the precooling heat exchanger 106 is divided into two paths to be respectively connected with inlets of a first shallow cooling heat exchanger 107 and a second shallow cooling heat exchanger 108, a gas path outlet of the first shallow cooling heat exchanger 107 is connected with an inlet of a first cryogenic heat exchanger 109, a gas path outlet of the second shallow cooling heat exchanger 108 is connected with an inlet of a second cryogenic heat exchanger 110, outlets of the first cryogenic heat exchanger 109 and the second cryogenic heat exchanger 110 are connected with an inlet of a gas-liquid separation tank 111 through a three-way reversing valve 204, a gas path outlet of the gas-liquid separation tank 111 is connected with an inlet of a gas fluorine heat exchanger 112, a gas path outlet of the gas fluorine heat exchanger 112 is connected with a cold side gas path inlet of the regenerative heat exchanger 105, and a cold side gas path outlet of the regenerative heat exchanger 105 reaches the standard and is discharged or is connected with a rear-stage process inlet.
As shown in fig. 2, the primary refrigeration system according to the present invention includes a primary refrigeration compressor 301 (explosion-proof refrigeration compressor), a primary oil separator 302 (high-efficiency oil separator), a primary condenser 303, a pre-cooling throttling element 304, a first throttling element 305, a second throttling element 306, and a primary gas-liquid separator 311; a refrigerant outlet of the primary refrigeration compressor 301 is connected with an inlet of the primary oil separator 302, a refrigerant outlet of the primary oil separator 302 is connected with a refrigerant inlet of the primary condenser 303, a refrigerant outlet of the primary condenser 303 is respectively provided with three heat exchange branches connected in parallel, outlets of the three heat exchange branches connected in parallel are respectively connected with an inlet of the primary gas-liquid separator 311, and the three heat exchange branches are connected to form a primary refrigeration cycle loop; the three parallel heat exchange paths are respectively a first heat exchange branch, a second heat exchange branch and a third heat exchange branch, the first heat exchange branch comprises a pre-cooling throttling element 304 and a pre-cooling heat exchanger 106 which are arranged at an inlet of the pre-cooling heat exchanger 106, the second heat exchange branch comprises a first throttling element 305 and a first shallow cooling heat exchanger 107 which are arranged at an inlet of the first shallow cooling heat exchanger 107, and the third heat exchange branch comprises a second throttling element 306 and a second shallow cooling heat exchanger 108 which are arranged at an inlet of the second shallow cooling heat exchanger 108. The first shallow cooling heat exchanger 107 and the second shallow cooling heat exchanger 108 of the primary refrigeration system are controlled by the primary refrigeration compressor 301, and can alternately cool and heat for defrosting. In the embodiment, the throttling element is an electronic expansion valve, so that the flow of the refrigerant can be accurately adjusted, the oil gas temperature of each stage of cold field can be effectively stabilized, and the small temperature fluctuation in the switching process of the device is ensured.
In the primary refrigeration system, two paths of defrosting systems (primary defrosting systems) are led out from the outlet of the primary oil separator, the high-temperature refrigerant inlet sent by a defrosting branch I (defrosting 1) is connected with the intermediate pipeline between the first control valve 307 and the first shallow cooling heat exchanger 107 through a first electromagnetic valve 901, and the low-temperature refrigerant outlet is connected with the intermediate pipeline between the first throttling element 305 and the first shallow cooling heat exchanger 107 through a third control valve 309; the high-temperature refrigerant inlet of the defrosting branch II (defrosting 2) is connected with the second control valve 308 and the intermediate pipeline of the second shallow cold heat exchanger 108 through a second electromagnetic valve 902, and the low-temperature refrigerant outlet is connected with the second throttling element 306 and the intermediate pipeline of the second shallow cold heat exchanger 108 through a fourth control valve 310. The low-temperature refrigerant in the first defrosting branch is sent to the outlet of the primary condenser 303 through the third control valve 309, and the low-temperature refrigerant in the second defrosting branch passes through the outlet of the primary condenser 303 through the fourth control valve 310.
As shown in fig. 3, the two-stage refrigeration system includes a two-stage refrigeration compressor 401 (explosion-proof refrigeration compressor), a two-stage oil separator 402, a two-stage condenser 403, a fifth throttling element 404, an evaporative condenser 600, and a two-stage gas-liquid separator 405; the refrigerant outlet of the secondary refrigeration compressor 401 is connected with the inlet of the secondary oil separator 402, the outlet of the secondary oil separator 402 is connected with the inlet of the secondary condenser 403, the secondary condenser 403 sends the refrigerant into the gas-fluorine heat exchanger 112 for heat exchange, the refrigerant sent out from the gas-fluorine heat exchanger 112 is sent into the evaporative condenser 600 again, the refrigerant sent out from the evaporative condenser 600 enters the secondary refrigeration compressor 401, and the fifth throttling element 404 is arranged between the outlet of the gas-fluorine heat exchanger 112 and the evaporation side inlet of the evaporative condenser 600.
The three-stage refrigeration system includes a three-stage refrigeration compressor 501 (explosion-proof refrigeration compressor), a three-stage oil separator 502 (high-efficiency oil separator) connected to the three-stage refrigeration compressor 501, an evaporative condenser 600 connected to the three-stage oil separator 502, a third throttling element 503, a fourth throttling element 504, a three-stage gas-liquid separator 509, and a switching control valve 510 provided at an inlet of the evaporative condenser 600. The three-stage refrigeration system is provided with two cryogenic heat exchange branches connected in parallel, wherein the first cryogenic heat exchange branch comprises a third throttling element 503 arranged at the inlet of the first cryogenic heat exchanger 109 and the first cryogenic heat exchanger 109, and the second cryogenic heat exchange branch comprises a fourth throttling element 504 arranged at the inlet of the second cryogenic heat exchanger 110 and the second cryogenic heat exchanger 110. The first cryogenic heat exchanger 109 and the second cryogenic heat exchanger 110 of the three-stage refrigeration system are controlled by the three-stage refrigeration compressor 501, and can alternately cool and heat for defrosting. The two-stage refrigeration system and the three-stage refrigeration system of the invention share the evaporative condenser 600, thereby forming a double-machine cascade refrigeration system.
In the three-stage refrigeration system, two defrosting systems (two-stage defrosting systems) are led out from the outlet of the three-stage oil separator 502, the high-temperature refrigerant inlet of a defrosting branch circuit III (defrosting 3) is connected with the fifth control valve 505 and the intermediate pipeline of the first cryogenic heat exchanger 109 through the third electromagnetic valve 903, and the low-temperature refrigerant outlet is connected with the third throttling element 503 and the intermediate pipeline of the first cryogenic heat exchanger 109 through the seventh control valve 507. The high-temperature refrigerant inlet of the defrosting branch line four (defrosting 4) is connected with the sixth control valve 506 and the intermediate pipeline of the second cryogenic heat exchanger 110 through a fourth electromagnetic valve 904, and the low-temperature refrigerant outlet is connected with the fourth throttling element 504 and the intermediate pipeline of the second cryogenic heat exchanger 110 through an eighth control valve 508. The low-temperature refrigerant in the defrosting branch circuit three is sent to the condensation side inlet of the evaporative condenser from the seventh control valve 507, the low-temperature refrigerant in the defrosting branch circuit four is sent to the condensation side inlet of the evaporative condenser from the eighth control valve 508, and the switching control valve 510 is arranged between the inlets of the refrigerants of the two defrosting systems and the refrigerant outlets of the two defrosting systems.
According to the invention, the differential pressure value and the operation time of the oil-gas channel are measured by the differential pressure transmitter, a proper oil-gas channel is selected, the continuity parameters of the device are ensured, such as the set differential pressure value of 20kPa and the set operation time of 12h, when either one of the two reaches the set value, the current channel is frozen and blocked, and the control system precools and then switches the other channel.
The control system matched with the oil gas system comprises a pressure transmitter 200 and a cut-off valve 201 which are arranged on an oil gas inlet pipeline, a first differential pressure transmitter 202 arranged between a first shallow cooling heat exchanger 107 and a first deep cooling heat exchanger 109, a second differential pressure transmitter 203 arranged between a second shallow cooling heat exchanger 108 and a second deep cooling heat exchanger 110, a three-way reversing valve 204 which is respectively communicated with the outlets of the first deep cooling heat exchanger 109 and the second deep cooling heat exchanger 110, and a control element 205(PLC) used for controlling the working state of the whole system; the pressure transmitter 200 and the air pump 103 of the control system are interlocked, the first differential pressure transmitter 202, the second differential pressure transmitter 203 and the three-way reversing valve 204 are linked, and the control element 205 organically integrates the oil gas system and the refrigeration system together, so that the automatic and reliable operation is realized.
In the invention, the first control valve 307, the second control valve 308, the third control valve 309, the fourth control valve 310, the fifth control valve 505, the sixth control valve 506, the seventh control valve 507 and the eighth control valve 508 are zero-leakage piston type pneumatic double-acting low-temperature cut-off valves 700 adopting multiple sealing protection, and are made of stainless steel materials integrally. The first to eighth control valves are a zero-leakage pneumatic double-acting piston low-temperature cut-off valve with multiple sealing protection and a meticulous control system, and small temperature fluctuation in the switching process of the device is guaranteed.
In addition, as a common knowledge in the field, the primary refrigeration system can also be provided with a liquid receiver and a drying filter after the primary condenser 303; similarly, the secondary refrigeration system may further include a liquid receiver and a dry filter after the secondary condenser 403; the three-stage refrigeration system can also be provided with a liquid receiver and a drying filter after the evaporative condenser 600.
As shown in fig. 4 to 6, the low temperature cut-off valve 700 has the structure: the valve comprises a valve body 701, a valve seat 702 arranged in the valve body 701, a valve core element 703 connected with the valve seat 702, a push rod 704 fixed with the upper end of the valve core element 703 and a cylinder 705 arranged at the top end of the push rod 704, wherein a valve cavity 706 is arranged on the periphery of the valve core element 703.
The valve body 701 has three sealed face, and the both ends are the import and the export of valve body 701 respectively, and the top is connection port, and the sealed terminal surface of the import of valve body 701 and export is the flange structure, and the flange structure chooses for use the loose flange in this embodiment, and the leakproofness is good, and corrosion-resistant easy maintenance installation again. The connection port of the valve body 701 is formed by a sealing surface formed by the valve seat 702, the chamber gasket 707, and the spool member 703, and the valve seat 702 is fixed to the spool member 703 by a second bolt 7021. The connecting port of the valve body 701 is a conventional static sealing surface, so that the leakage hidden danger is avoided.
Specifically, a passage 7011 that is opened or closed by moving the valve seat 702 up and down is provided between the inlet and the outlet of the valve body 701 according to the present invention. A mounting hole through which a bolt passes is formed in the middle of the valve seat 702, the second bolt 7021 is fixed to the valve element 703 through the mounting hole, and a step connected to the valve element 7033 is formed in the wall of the upper end surface (connection port) of the valve body 701.
The valve core element 703 comprises a connecting rod 7031, a bellows segment 7032, a valve core 7033 arranged at the lower end of the bellows segment 7032, and a sealing plate 7034 arranged at the upper end of the bellows segment 7032, wherein one end of the connecting rod 7031 is fixedly connected with the valve seat 702 through a second bolt 1021, and the top end of the connecting rod 7031 is fixed with the push rod 704. As shown in fig. 4 to 6, the inner diameters of the valve core 7033 and the connection port 7012 of the valve body 701 are equal to each other, so that the connection port is sealed, and meanwhile, a valve cavity gasket 707 is arranged at the connection position of the valve core 7033 and the valve body 701, so that the sealing effect is enhanced, and leakage is prevented. The connecting rod 7031 passes through the valve core 7033 and is fixed with the push rod 704. In order to prevent a part of refrigerant from entering the valve body 706 through a gap between the connecting rod 7031 and the valve body 7031 when the connecting rod 7031 moves up and down, according to the present invention, a segment of bellows segment 7032 is disposed above the valve core 7033, the bellows segment 7032 is sleeved on the periphery of the connecting rod 7031, the bottom end of the bellows segment 7032 is fixedly sealed with the upper surface of the valve core 7033, and the upper end of the valve core 7033 is fixedly sealed with the sealing plate 7034, such that the upward-fleeing refrigerant enters a cavity formed between the bellows segment 7032 and the connecting rod 7031, and the sealing plate 7034 and the connecting rod 7031 are completely sealed, and the sealing plate 7034 moves up and down along with the connecting rod 7031, so as to ensure that the refrigerant does not leak from between the sealing plate 7034 and the connecting rod 7031. Closure plate 7034 serves to secure bellows segment 7032 and also to seal. The outer diameter of the sealing plate 7034 fits against the inner wall of the valve chamber 706 and can move up and down along the inner wall of the valve chamber 706. The bellows segment 7032 provided to the spool element 703 has excellent elastic displacement amount and rigidity; when the valve is opened, the medium refrigerant is in a cavity formed by the corrugated pipe joint 7032 and the connecting rod 7031, and the volume change caused by the quenching and sudden heating of the refrigerant is automatically compensated and eliminated by the corrugated pipe, so that the leakage is avoided, and the service life of the valve is prolonged. The bottom end (lower end surface) of the valve chamber 706 provided on the outer periphery of the valve element 703 is of a flange structure, and the lower end surface of the valve chamber 706 is fixed to the sealing end surface of the valve body 701 by a first bolt 1061. The top (upper end) of the valve cavity 706 is provided with a first connecting flange 708, and the first connecting flange 708 is fixed with the lower cylinder cover 7053 through a first upright column 7062.
The cylinder 705 comprises a cylinder sleeve 7051, an upper cylinder cover 7052 and a lower cylinder cover 7053 which are arranged at the upper end and the lower end of the cylinder sleeve 7051, a first air source interface 7054 arranged on the upper cylinder cover 7052, a second air source interface 7055 arranged on the lower cylinder cover 7053, and a piston 7056 arranged in the cylinder sleeve 7051, wherein the bottom end of the piston 7056 is connected with a push rod 704, a piston ring 7057 is arranged between the piston 7056 and the inner wall of the cylinder 705, and the upper cylinder cover 7052 and the lower cylinder cover 7053 are fixed through a second bolt 7058.
The top of the valve cavity 706 is fixed with the bottom end of the push rod 704 through a first nut 7066, and in addition, a dust ring 7063, a packing 7064 and an O-shaped ring 7065 are arranged between the top of the valve cavity 706 and the push rod 704.
The working method of the piston type pneumatic low-temperature switching valve comprises the following steps: the upper cylinder cover 7052 is provided with a first air source port 7054, the first air source port 7054 receives an input signal, instrument wind is introduced into the port, the piston 7056 is pressed down by pressure, the push rod 704, the valve core element 703 and the valve seat 702 are driven, and the valve seat 702 is moved to the limit position to close the switching valve; the lower cylinder cover 7053 is provided with a second air supply port 7055, the second air supply port 7055 receives an input signal, instrument air is introduced into the second air supply port 7055, the piston 7056 is pushed up by pressure, the push rod 704, the valve element 703 and the valve seat 702 are driven, and the valve seat 702 is separated from a central channel of the valve body 701 to open the switching valve. The low-temperature switching valve can be used with the electromagnetic valve, and the low-temperature switching valve controls instrument air through the electromagnetic valve so as to control the low-temperature switching valve to be opened, so that the low-temperature switching valve is more convenient to control and quick in response.
The fluid medium passed by the switching valve is refrigerant, the working temperature range of the switching valve is from-100 ℃ to 120 ℃, the working temperature can instantly rise from the lowest point to the highest point and can also fall from the highest point to the lowest point, and the switching valve can bear the thermal stress change caused by rapid cooling and sudden heating at-100 ℃ to 120 ℃ through the arrangement of the corrugated pipe joints, so that the stability of the piston type pneumatic low-temperature switching valve is improved; and the first sealing of the refrigerant is realized through the fixed valve core, the refrigerant entering from the valve core is sealed in a cavity formed by the corrugated pipe joint and the connecting rod through the sealing plate, the second sealing is realized, the air leakage of the inlet side and the outlet side is tight when the valve is closed, and simultaneously, the medium in the valve body has zero leakage to the outside.
The oil gas recovery of the oil tanker dock is carried out under the condition that the channel A is smooth:
when the primary refrigeration system works, high-temperature and high-pressure refrigerant gas discharged by a primary refrigeration compressor 301 enters a primary condenser 303 after being subjected to oil separation by a primary oil separator 302 to be condensed into high-pressure refrigerant liquid, the high-temperature and high-pressure refrigerant gas is subjected to pressure reduction by a pre-cooling throttling element 304 and a first throttling element 305 in two paths to form low-temperature and low-pressure vapor-liquid two-phase mixture, the low-temperature and low-pressure vapor-liquid two-phase mixture respectively enters the pre-cooling heat exchanger 106 and the first shallow cooling heat exchanger 107, the low-temperature and low-pressure vapor-liquid two-phase mixture is evaporated in the pre-cooling heat exchanger 106 and the first shallow cooling heat exchanger 107 and absorbs oil gas heat passing through the pre-cooling heat exchanger 106 and the first shallow cooling heat exchanger 107, so that oil gas flowing through the pre-cooling heat exchanger 106 and the first shallow cooling heat exchanger 107 is cooled and liquefied, and the refrigerant is compressed by the primary refrigeration compressor 301 through a primary gas-liquid separator 311 to enter the next cycle after being fully vaporized;
high-temperature and high-pressure refrigerant gas discharged by the secondary refrigeration compressor 401 enters a secondary condenser 403 after being subjected to oil separation by a secondary oil separator 402 to be condensed into high-pressure refrigerant liquid, the cold energy of low-temperature oil gas is absorbed by a gas-fluorine heat exchanger 112 to form subcooled refrigerant liquid, the subcooled refrigerant liquid is decompressed by a fifth throttling element 404 to form low-temperature and low-pressure gas-liquid two-phase mixture, the mixture enters an evaporative condenser 600, the mixture is evaporated in the evaporative condensing heat exchanger 600 and absorbs the heat of the high-temperature and high-pressure refrigerant discharged by a third refrigeration compressor 501 (an explosion-proof refrigeration compressor) therein, so that the refrigerant flowing through the third-stage system is condensed, and the refrigerant is compressed by the secondary refrigeration compressor 401 through a secondary gas-liquid separator 405 after being fully vaporized and enters the next cycle;
high-temperature and high-pressure refrigerant gas discharged by the third refrigeration compressor 501 is subjected to oil separation by the three-stage oil separator 502, then enters the evaporative condensation heat exchanger 600 through the switching control valve 510 to be condensed into high-pressure supercooled refrigerant liquid, is throttled and reduced into low-temperature and low-pressure vapor-liquid two-phase mixture by the third throttling element 503, enters the first cryogenic heat exchanger 109, is evaporated in the first cryogenic heat exchanger 109 and absorbs heat of oil gas passing through the first cryogenic heat exchanger 109, so that the oil gas flowing through the first cryogenic heat exchanger 109 is further cooled and liquefied, and the refrigerant is compressed by the third explosion-proof refrigeration compressor 501 through the three-stage gas-liquid separator 509 after being fully vaporized and enters the next cycle.
The oil gas recovery of the oil tanker dock is defrosted by the following method under the condition that the channel B is frozen and blocked:
(S21) obtaining a command to be switched by a control system, firstly separating part of refrigerant (1/7-1/5 refrigerant) to pre-cool the spare oil-gas channel in advance, and then switching when the spare channel reaches a set temperature, wherein the temperature fluctuation in the switching process can be controlled to be +/-4 ℃.
(S22) when the primary defrosting system works, high-temperature and high-pressure refrigerant gas discharged by the primary refrigeration compressor 301 is subjected to oil separation by the primary oil separator 302 and then enters the second shallow-cooling heat exchanger 108 through the second electromagnetic valve 902, solid oil attached to the surface of the heat exchange tube in the second shallow-cooling heat exchanger 108 absorbs heat of the refrigerant to defrost, so that the second shallow-cooling heat exchanger 108 absorbs heat to defrost for standby, and the refrigerant liquid is condensed into high-pressure refrigerant liquid, then is merged with condensate of the primary condenser 303 through the fourth control valve 310, and then enters the system circulation.
When the second-stage defrosting system works, high-temperature and high-pressure refrigerant gas discharged by the third refrigeration compressor 501 is subjected to oil separation by the second-stage oil separator 502 and then enters the second cryogenic heat exchanger 110 through the fourth electromagnetic valve 904, solid oil attached to the surface of the heat exchange tube in the second cryogenic heat exchanger 110 absorbs heat of the refrigerant to defrost, so that the second cryogenic heat exchanger 110 absorbs heat to defrost for standby, and the refrigerant gas is condensed into high-pressure refrigerant liquid, then is connected to the evaporation and condensation heat exchanger 600 through the eighth control valve 508 and then enters the system circulation.
Similarly, under the condition that the channel A is frozen and blocked, defrosting is carried out on the channel A by controlling the first defrosting branch and the third defrosting branch, and the rest working methods are the same as those of the channel B.
The condensed and separated liquid oil is led to an oil collecting tank from a bottom oil outlet, and the low-concentration oil gas can be directly discharged up to the standard or enter the next link, such as: an adsorption section and an oxidation catalysis section for further purification treatment.
Example 2: the throughput was 300m3Oil gas recovery device for oil tanker wharf, wherein oil gas is volatile oil gas of finished oil, and inlet gas concentration is 1000g/m3The wharf oil gas recovery device distributed in the market at present is formed by combining two sets of single-path condensation oil gas recovery systems at the temperature of 70 ℃ below zero, the power of an air pump is 5.5kW, the power of the single-path condensation system is 49.4kW, the total unit power is 104.3kW, and the unit energy consumption is 0.348 kW/(m) m3/h)。
300m of the invention3The final oil gas temperature of the oil tanker wharf oil gas recovery device is-70 ℃, the air pump is the Shandong Fengyuan explosion-proof Roots air pump with the power of 5.5kW, the first-stage explosion-proof compressor of the two-way condensation system is the German Bitzer piston compressor 4GE-23Y with the power of 14.3kW, the second-stage explosion-proof compressor is the China Taiwan Fusheng screw compressor CSR170-Ex with the power of 34.6kW, the third-stage explosion-proof compressor is the German Bitzer piston compressor 6HE-28Y with the power of 12.4kW, the explosion-proof axial flow fan for the air-cooled heat exchanger is Suzhou Rui with the power of 4.0kW, the total unit power is 70.8kW, and the unit energy consumption is 0.236kW/(m3H), the energy efficiency is improved by 47.5 percent.
As described above, although the oil and gas recovery device in the oil tanker terminal according to the present invention has been shown and described with reference to the specific preferred embodiment, the present invention is not limited to the pure condensing oil and gas recovery device, and may be changed to a combination of condensing + adsorbing, condensing + absorbing, and may further include an oxidation catalytic function, etc., all of which are within the protection scope of the present invention. Various changes in form and details may be made therein without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (10)
1. A method for recovering oil and gas in an oil tanker wharf is characterized by comprising the following steps:
(S1) sending the oil gas to be processed, which is sent from the oil gas inlet, into the oil gas system, sequentially passing through a regenerative heat exchanger, a precooling heat exchanger, a shallow cooling heat exchanger, a deep cooling heat exchanger and a gas fluorine heat exchanger in the oil gas system, liquefying the oil gas by exchanging heat with a refrigerant sent out by a refrigeration system, sending the oil gas processed by the gas fluorine heat exchanger into the regenerative heat exchanger again, and discharging the oil gas after exchanging heat in the regenerative heat exchanger;
(S2) the refrigeration system includes a primary refrigeration system, a secondary refrigeration system, and a tertiary refrigeration system; the primary refrigeration system respectively sends the refrigerant into the precooling heat exchanger and the shallow cooling heat exchanger to exchange heat with oil gas; the secondary refrigeration system sends the refrigerant into a gas-fluorine heat exchanger to exchange heat with oil gas, and the refrigerant after heat exchange is sent into an evaporative condenser; the three-stage refrigeration system sends the refrigerant into the cryogenic heat exchanger to exchange heat with the oil gas, and the refrigerant after heat exchange returns to a refrigeration compressor of the three-stage refrigeration system to carry out refrigeration cycle;
(S3) when the system needs defrosting, the high-temperature high-pressure refrigerant sent from the first-stage refrigeration system is sent to the shallow cooling heat exchanger for defrosting, and the high-temperature high-pressure refrigerant sent from the third-stage refrigeration system is sent to the deep cooling heat exchanger for defrosting.
2. The tanker dock oil and gas recovery method of claim 1, wherein said shallow cold heat exchanger comprises a first shallow cold heat exchanger and a second shallow cold heat exchanger arranged in parallel; the cryogenic heat exchanger comprises a first cryogenic heat exchanger and a second cryogenic heat exchanger which are arranged in parallel.
3. The oil and gas recovery method for the oil tanker dock according to claim 2, wherein the primary refrigeration system comprises a primary refrigeration compressor and a primary condenser connected to a refrigerant outlet of the primary refrigeration compressor, and an outlet of the primary condenser is connected to inlets of the pre-cooling heat exchanger, the first shallow cooling heat exchanger and the second shallow cooling heat exchanger respectively; the secondary refrigeration system comprises a secondary refrigeration compressor, a secondary condenser and an evaporative condenser, wherein the secondary condenser is connected with the outlet of the secondary refrigeration compressor; an outlet of the secondary condenser is connected with a refrigerant inlet of the gas-fluorine heat exchanger, and an evaporation side inlet of the evaporative condenser is connected with an outlet of the gas-fluorine heat exchanger; the three-stage refrigeration system comprises a three-stage refrigeration compressor and an evaporative condenser connected with the three-stage refrigeration compressor; and the outlet of the condensation side of the evaporative condenser is respectively connected with the inlets of the first cryogenic heat exchanger and the second cryogenic heat exchanger.
4. The oil-gas recovery method for the oil tanker dock according to claim 3, wherein two defrosting branches are respectively led out from an outlet of the primary compressor and connected with the first shallow-cooling heat exchanger and the second shallow-cooling heat exchanger; and a condensation side inlet of the evaporative condenser is respectively led out two defrosting branches to be connected with the first cryogenic heat exchanger and the second cryogenic heat exchanger.
5. The oil and gas recovery method for the oil tanker dock according to claim 4, wherein the refrigerant sent by the two defrosting branches led out from the outlet of the primary compressor is merged with the refrigerant sent by the outlet of the primary condenser; and two defrosting branches led out from the condensation side inlet of the evaporative condenser are used for converging the refrigerant after heat exchange with the refrigerant sent into the evaporative condenser again.
6. The oil and gas recovery method for the oil tanker dock according to claim 5, wherein a switching control valve is arranged between an inlet of the two defrosting branches led out from the condensation side of the evaporative condenser and an outlet of the two defrosting branches.
7. The oil and gas recovery method for the oil tanker dock according to claim 6, wherein an inlet of said pre-cooling heat exchanger is provided with a pre-cooling throttling element, an inlet of said first shallow cooling heat exchanger is provided with a first throttling element, and an inlet of said second shallow cooling heat exchanger is provided with a second throttling element; a third throttling element is arranged between the outlet of the condensation side of the evaporative condenser and the inlet of the first cryogenic heat exchanger, and a fourth throttling element is arranged between the outlet of the condensation side of the evaporative condenser and the inlet of the second cryogenic heat exchanger; and a fifth throttling element is arranged between the outlet of the gas-fluorine heat exchanger and the evaporation side inlet of the evaporative condenser.
8. The tanker dock vapor recovery method of claim 4, wherein a first control valve is disposed between the outlet of the primary compressor and the first shallow cold heat exchanger, and a second control valve is disposed between the outlet of the primary compressor and the second shallow cold heat exchanger; the outlets of the first shallow cooling heat exchanger and the second shallow cooling heat exchanger are respectively provided with a third control valve and a fourth control valve; a fifth control valve is arranged between the condensation side inlet of the evaporative condenser and the first cryogenic heat exchanger, and a sixth control valve is arranged between the condensation side inlet of the evaporative condenser and the second cryogenic heat exchanger; and the outlets of the first cryogenic heat exchanger and the second cryogenic heat exchanger are respectively provided with a seventh control valve and an eighth control valve.
9. Tanker dock oil and gas recovery method according to claim 1, wherein the oil and gas system is provided with a control system comprising a pressure transmitter and a shut-off valve arranged at an oil and gas inlet.
10. The method for tanker dock vapor recovery according to claim 2, wherein a first differential pressure transmitter is disposed between said first shallow cold heat exchanger and said first cryogenic heat exchanger; and a second differential pressure transmitter is arranged between the second shallow cooling heat exchanger and the second deep cooling heat exchanger.
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