CN114699788B - Oil gas recovery method for oil tanker wharf - Google Patents
Oil gas recovery method for oil tanker wharf Download PDFInfo
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- CN114699788B CN114699788B CN202210261673.7A CN202210261673A CN114699788B CN 114699788 B CN114699788 B CN 114699788B CN 202210261673 A CN202210261673 A CN 202210261673A CN 114699788 B CN114699788 B CN 114699788B
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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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Abstract
The invention discloses a method for recovering oil gas of a tanker wharf, which comprises the following steps: the oil gas to be treated, which is sent 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 Leng Huanre device, a cryogenic 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 refrigerating system, and is sent into the regenerative heat exchanger again after being treated by the gas fluorine heat exchanger, and is discharged after being subjected to heat exchange in the regenerative heat exchanger; when the system needs defrosting, the high-temperature and high-pressure refrigerant is sent to the shallow Leng Huanre device and the cryogenic heat exchanger for defrosting. The invention not only ensures the fluctuation of the cold field temperature of the oil and gas recovery device of the oil tanker wharf to +/-4 ℃, but also improves the energy efficiency by more than 40%.
Description
Technical Field
The invention belongs to the technical field of oil gas recovery, and particularly relates to an oil gas recovery method for a tanker wharf.
Background
The construction start of the wharf oil gas recovery facility is late, and the practical running experience is insufficient. And then the oil gas recovery of the crude oil wharf is steadily promoted in coasts, more and more oil gas recovery facilities are installed in the wharf, and the continuous operation of the oil gas recovery facilities of the wharf can basically meet the continuity of shipping, but the use effect is uneven and the energy consumption is larger. The prior art such as a wharf oil gas recovery device (CN 2013104309861) solves the problem of continuous operation of the device, but for the waste gas of the chemical VOCs, the wharf cannot continuously operate for 24 hours due to deep cooling without a standby cold field. And the existing oil gas recovery facilities of the wheel oil wharf have large oil gas temperature fluctuation and larger energy consumption of a unit.
Disclosure of Invention
The invention aims to: in order to solve the problems in the prior art, the invention provides a method for recovering oil gas of a tanker wharf, and the method can realize continuous oil gas recovery, and simultaneously has small oil gas temperature fluctuation and low energy consumption.
The technical scheme is as follows: the invention relates to a method for recovering oil gas of a tanker wharf, which comprises the following steps:
(S1) the oil gas to be treated fed from the oil gas inlet is fed into an oil gas system, sequentially passes through a regenerative heat exchanger, a precooling heat exchanger, a shallow Leng Huanre device, a cryogenic heat exchanger and a gas fluorine heat exchanger in the oil gas system, liquefies the oil gas through heat exchange with a refrigerant fed out of a refrigerating system, and feeds the oil gas treated by the gas fluorine heat exchanger into the regenerative heat exchanger again, exchanges heat in the regenerative heat exchanger and is discharged;
(S2) the refrigeration system comprises a primary refrigeration system, a secondary refrigeration system and a tertiary refrigeration system; the primary refrigeration system sends the refrigerant into a pre-cooling heat exchanger and a shallow Leng Huanre device to exchange heat with oil gas; the second-stage refrigerating 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 evaporation condenser; the three-stage refrigerating system sends the refrigerant into a cryogenic heat exchanger to exchange heat with oil gas, and the refrigerant after heat exchange returns to a refrigerating compressor of the three-stage refrigerating system to perform refrigerating cycle;
and (S3) when the system needs to defrost, the high-temperature and high-pressure refrigerant sent out from the primary refrigeration system is sent into the shallow-cooling heat exchanger to defrost, and the high-temperature and high-pressure refrigerant sent out from the tertiary refrigeration system is sent into the deep-cooling heat exchanger to defrost.
As a preferred embodiment of the present invention, the shallow-cooling heat exchanger includes a first shallow-cooling heat exchanger and a second shallow Leng Huanre unit arranged in parallel; the cryogenic heat exchanger comprises a first cryogenic heat exchanger and a second cryogenic heat exchanger which are arranged in parallel.
Specifically, 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 air passage outlet of the regenerative heat exchanger, a first shallow-cooling heat exchanger and a second shallow Leng Huanre device which are respectively connected with an air passage outlet of the precooling heat exchanger, a first cryogenic heat exchanger connected with an air passage outlet of the first shallow-cooling heat exchanger, a second cryogenic heat exchanger connected with an air passage 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 an air passage outlet of the gas-liquid separation tank, and a regenerative heat exchanger connected with an air passage 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 evaporation condenser, wherein the secondary condenser is connected with an outlet of the secondary refrigeration compressor; the outlet of the secondary condenser is connected with the refrigerant inlet of the gas-fluorine heat exchanger, and the evaporation side inlet of the evaporation condenser is connected with the outlet of the gas-fluorine heat exchanger; the three-stage refrigeration system comprises a three-stage refrigeration compressor and an evaporation condenser connected with the three-stage refrigeration compressor; and the condensation side outlet of the evaporation condenser is respectively connected with the inlets of the first cryogenic heat exchanger and the second cryogenic heat exchanger.
As a preferred implementation mode of the invention, the outlet of the primary compressor is respectively led out of two branches of defrosting, and is connected with the first shallow cooling heat exchanger and the second shallow cooling heat exchanger; and the condensation side inlet of the evaporation condenser is respectively led out of two paths of defrosting branches to be connected with the first cryogenic heat exchanger and the second cryogenic heat exchanger.
As a preferred embodiment of the present invention, the refrigerant sent out by the two defrosting branches led out from the outlet of the first-stage compressor is converged with the refrigerant sent out by the outlet of the first-stage condenser; and the two defrosting branches led out from the inlet of the condensing side of the evaporative condenser are used for merging the refrigerant after heat exchange with the refrigerant sent into the evaporative condenser again.
As a preferred embodiment of the invention, a switching control valve is arranged between the inlets of the two defrosting branches led out from the condensation side of the evaporative condenser and the outlets of the two defrosting branches.
As a preferred embodiment of the present invention, the inlet of the pre-cooling heat exchanger is provided with a pre-cooling throttling element, the inlet of the first shallow cooling heat exchanger is provided with a first throttling element, and the inlet of the second shallow cooling heat exchanger is provided with a second throttling element; a third throttling element is arranged between the condensing side outlet of the evaporative condenser and the inlet of the first cryogenic heat exchanger, and a fourth throttling element is arranged between the condensing side outlet 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 inlet of the evaporation side of the evaporation 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 condensing side inlet of the evaporative condenser and the first cryogenic heat exchanger, and a sixth control valve is arranged between the condensing 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 invention, the oil and gas system is also provided with a control system in a matched manner, wherein the control system comprises a pressure transmitter and a shut-off valve which are arranged between the oil and gas inlet and the air pump. The control system of the invention also comprises a first differential pressure transmitter and a second differential pressure transmitter, and further comprises a three-way reversing valve of a control loop and a control element, wherein the control element is preferably a PLC control module, and Siemens control software or GE and other control software are integrated.
As a preferred embodiment of the present invention, the first to eighth control valves described in the present invention are all pneumatically double-acting cryogenic shut-off valves.
The invention relates to a low-temperature switching valve, which 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 a cylinder arranged at the top end of the push rod, wherein the periphery of the valve core element is a valve cavity; the valve core element comprises a connecting rod, a corrugated pipe joint arranged on the periphery of the connecting rod, a valve core arranged at the lower end of the corrugated pipe joint and a sealing plate arranged at the upper end of the corrugated pipe joint, wherein the sealing plate is sealed with the connecting rod.
As a preferred embodiment of the invention, the cylinder comprises a cylinder sleeve, an upper cylinder cover, a lower cylinder cover, a first air source interface, a second air source interface and a piston, wherein the upper cylinder cover and the lower cylinder cover are arranged at the upper end and the lower end of the cylinder sleeve; and/or the valve body is fixed with the valve cavity through a first bolt.
As a preferred embodiment of the present invention, the bellows joint includes a connection section, a fixing plate, and a bellows section provided between the valve element and the fixing plate.
As a preferred embodiment of the invention, the valve seat is fixed to the valve element by a second bolt.
As a preferred embodiment of the invention, a valve chamber gasket is arranged between the valve core element and the valve body.
As 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 the top end of the valve cavity, and the first connecting flange is fixed to the lower cylinder cover through a first upright post.
As a preferred embodiment of the invention, a dust ring, a filler and an O-ring are arranged between the top of the valve cavity and the push rod.
As a preferred embodiment of the invention, the top of the valve cavity and the bottom end of the push rod are fixed through a first nut.
As a preferred embodiment of the present invention, a piston ring is provided between the piston and the inner wall of the cylinder.
As a preferred embodiment of the present invention, the upper cylinder head and the lower cylinder head are fixed 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 deep-cooling heat exchanger; a second differential pressure transmitter is arranged between the second shallow Leng Huanre device and the second cryogenic heat exchanger.
Preferably, the backheating heat exchanger is a cold field heat exchanger at 30 ℃, so that hidden danger of ice blockage is avoided; the precooling heat exchanger is a 4 ℃ (adjustable) cold field heat exchanger, and has no hidden danger of ice blockage; the first shallow heat exchanger A and the second shallow Leng Huanre device B are-25 ℃ (adjustable) cold field heat exchangers; the first cryogenic heat exchanger and the second cryogenic heat exchanger are-70 ℃ (adjustable) cold field heat exchangers.
The beneficial effects are that: (1) According to the invention, by arranging different heat exchangers, the heat exchanger is ensured to have no ice blockage risk in normal operation in the oil gas recovery treatment process, and the regenerative heat exchanger regenerates heat by utilizing temperature difference, so that frosting is avoided; the temperature of the precooling heat exchanger is controlled to be higher than the dew point temperature of 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 removed by a tube side, the oil gas is in a temperature rise process, frosting is avoided, the cold energy is absorbed by the refrigerant of the second refrigerating system, and the gas-fluorine heat exchanger is used for supercooling to improve the refrigerating energy efficiency; (2) According to the invention, the shallow Leng Huanre device and the cryogenic heat exchanger with ice blockage hidden danger are arranged as two paths, the oil gas system is divided into an A path and a B path, one path works normally and the other path is standby, so that the whole device can be ensured to run continuously; the continuous operation requirement of the oil and gas recovery facility of the oil tanker wharf is met; (3) According to the invention, differential pressure transmitters are further arranged between the shallow Leng Huanre devices and the cryogenic heat exchangers of the channel A and the channel B respectively, the differential pressure value and the running time of the oil-gas channel are measured, and the proper oil-gas channel is selected, so that the continuity of the device is ensured; (4) The temperature fluctuation in the oil gas recovery process is small, and the throttling element can accurately adjust the flow of the refrigerant for the electronic expansion valve so as to effectively stabilize the oil gas temperature of cold fields at all levels; secondly, the control valve adopts a zero-leakage pneumatic double-acting piston low-temperature cut-off valve with multiple seal protection, so that external leakage of the refrigerant is avoided, internal leakage of the refrigerant is avoided, and further temperature fluctuation is maintained; finally, when the channel is switched, the device pre-cools 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 in the switching process can be controlled to be +/-4 ℃. (6) the oil gas recovery energy consumption of the invention is low: the device is provided with a regenerative heat exchanger for primary energy recovery, a gas-fluorine heat exchanger for reducing the supercooling degree of the refrigerant and improving the energy efficiency of the refrigeration compressor, and an oil-cooling recoverer for improving the energy efficiency of the refrigeration compressor is arranged at the bottoms of the precooling heat exchanger, the shallow Leng Huanre device and the deep cooling heat exchanger; (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%.
Drawings
FIG. 1 is a schematic diagram of an oil and gas system of a tanker dock oil and gas recovery apparatus of the present invention;
FIG. 2 is a schematic diagram of a primary refrigeration system of the oil and gas recovery apparatus of the tanker dock of the present invention;
FIG. 3 is a schematic diagram of a two-stage refrigeration and three-stage refrigeration system of the oil and gas recovery apparatus of the present invention for a tanker dock;
FIG. 4 is an exploded view of the cryogenic switching valve of the present invention;
FIG. 5 is a cross-sectional view of a spool element in the low temperature shift valve of the present invention;
fig. 6 is a cross-sectional view of the cryogenic switching valve of the invention.
Detailed Description
Example 1: as shown in fig. 1-3, the oil and gas recovery method for the oil tanker wharf of the invention comprises the following steps:
(S1) the oil gas to be treated fed from the oil gas inlet is fed into an oil gas system, sequentially passes through a regenerative heat exchanger, a precooling heat exchanger, a shallow Leng Huanre device, a cryogenic heat exchanger and a gas fluorine heat exchanger in the oil gas system, liquefies the oil gas through heat exchange with a refrigerant fed out of a refrigerating system, and feeds the oil gas treated by the gas fluorine heat exchanger into the regenerative heat exchanger again, exchanges heat in the regenerative heat exchanger and is discharged;
(S2) the refrigeration system comprises a primary refrigeration system, a secondary refrigeration system and a tertiary refrigeration system; the primary refrigeration system sends the refrigerant into a pre-cooling heat exchanger and a shallow Leng Huanre device to exchange heat with oil gas; the second-stage refrigerating 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 evaporation condenser; the three-stage refrigerating 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 refrigerating compressor of the three-stage refrigerating system to be subjected to refrigerant circulation;
and (S3) when the system needs to defrost, the high-temperature and high-pressure refrigerant sent out from the primary refrigeration system is sent into the shallow-cooling heat exchanger to defrost, and the high-temperature and high-pressure refrigerant sent out from the tertiary refrigeration system is sent into the deep-cooling heat exchanger to defrost.
Specifically, the oil-gas system of the invention comprises a first flame arrester 101, a condensate tank 102, an air pump 103, a second flame arrester 104, a backheating heat exchanger 105, a precooling heat exchanger 106, a first shallow-cooling heat exchanger 107, a second shallow Leng Huanre 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 inlet of the condensate tank 102 is connected with an oil gas inlet, the outlet of the condensate tank 102 is connected with the inlet of the air pump 103, the outlet of the air pump 103 is connected with the hot side gas path inlet of the regenerative heat exchanger 105, a first flame arrester 101 is arranged between the inlet of the condensate tank 102 and the oil gas inlet, a second flame arrester 104 is arranged between the outlet of the air pump 103 and the hot side gas path inlet of the regenerative heat exchanger 105, in the embodiment, the air pump 103 is an explosion-proof variable-frequency Roots air pump, the first flame arrester 101 is an explosion-proof flame arrester, and the second flame arrester 104 is an explosion-proof flame arrester.
The oil gas is sent into the back-heating heat exchanger 105 under the action of the air pump 103, the hot side air channel outlet of the back-heating heat exchanger 105 is connected with the inlet of the pre-cooling heat exchanger 106, the air channel outlet of the pre-cooling heat exchanger 106 is connected with the inlet of the first shallow cooling heat exchanger 107 and the inlet of the second shallow Leng Huanre heat exchanger 108 respectively in two channels, the air channel outlet of the first shallow cooling heat exchanger 107 is connected with the inlet of the first cryogenic heat exchanger 109, the air channel outlet of the second shallow Leng Huanre heat exchanger 108 is connected with the inlet of the second cryogenic heat exchanger 110, the outlets of the first cryogenic heat exchanger 109 and the second cryogenic heat exchanger 110 are connected with the inlet of the gas-liquid separation tank 111 through the three-way reversing valve 204, the air channel outlet of the gas-liquid separation tank 111 is connected with the inlet of the gas-fluorine heat exchanger 112, the air channel outlet of the gas-fluorine heat exchanger 112 is connected with the cold side air channel inlet of the back-heating heat exchanger 105, and the cold side air channel outlet of the heat exchanger 105 is discharged up to the standard or connected with the inlet of the back-stage process.
As shown in fig. 2, the primary refrigeration system of 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; the refrigerant outlet of the first-stage refrigeration compressor 301 is connected with the inlet of the first-stage oil separator 302, the refrigerant outlet of the first-stage oil separator 302 is connected with the refrigerant inlet of the first-stage condenser 303, the refrigerant outlet of the first-stage condenser 303 is respectively provided with three parallel heat exchange branches, and the outlets of the three parallel heat exchange branches are respectively connected with the inlet of the first-stage gas-liquid separator 311 to form a first-stage refrigeration cycle; the three parallel heat exchange paths are a first heat exchange branch, a second heat exchange branch and a third heat exchange branch, wherein the first heat exchange branch comprises a pre-cooling throttling element 304 and a pre-cooling heat exchanger 106 which are arranged at the 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 the 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 Leng Huanre which are arranged at the inlet of the second shallow Leng Huanre. The first shallow cold heat exchanger 107 and the second shallow Leng Huanre device 108 of the primary refrigeration system are controlled by the primary refrigeration compressor 301, and can alternately cool and heat and defrost. (in the embodiment, the throttling element is an electronic expansion valve, so that the flow of the refrigerant can be accurately regulated to effectively stabilize the oil gas temperature of cold field at each level, and the temperature fluctuation in the switching process of the device is ensured to be small).
In the primary refrigeration system, a two-way defrosting system (primary defrosting system) is led out from an outlet of a primary oil separator, a high-temperature refrigerant inlet sent out by a defrosting branch I (defrosting 1) is connected with a first control valve 307 and a middle pipeline of a first shallow-cooling heat exchanger 107 through a first electromagnetic valve 901, and a low-temperature refrigerant outlet is connected with a first throttling element 305 and a middle pipeline of the first shallow-cooling heat exchanger 107 through a third control valve 309; the high-temperature refrigerant inlet of the second defrosting branch (defrosting 2) is connected with the second control valve 308 and the middle pipeline of the second shallow Leng Huanre device 108 through the second electromagnetic valve 902, and the low-temperature refrigerant outlet is connected with the second throttling element 306 and the middle pipeline of the second shallow Leng Huanre device 108 through the fourth control valve 310. The low-temperature refrigerant in the first defrosting branch is sent out to the outlet of the first-stage condenser 303 through the third control valve 309, and the low-temperature refrigerant in the second defrosting branch is sent out to the outlet of the first-stage condenser 303 through the fourth control valve 310.
As shown in fig. 3, the secondary refrigeration system includes a secondary refrigeration compressor 401 (explosion-proof refrigeration compressor), a secondary oil separator 402, a secondary condenser 403, a fifth throttling element 404, an evaporative condenser 600, and a secondary gas-liquid separator 405; the refrigerant outlet of the second-stage refrigeration compressor 401 is connected to the inlet of the second-stage oil separator 402, the outlet of the second-stage oil separator 402 is connected to the inlet of the second-stage condenser 403, the second-stage condenser 403 sends the refrigerant into the gas-fluorine heat exchanger 112 to exchange heat, the refrigerant sent out from the gas-fluorine heat exchanger 112 is sent into the evaporation condenser 600 again, the refrigerant sent out from the evaporation condenser 600 enters the second-stage refrigeration compressor 401, and the fifth throttling element 404 is disposed between the outlet of the gas-fluorine heat exchanger 112 and the evaporation-side inlet of the evaporation 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 and defrost. The two-stage refrigeration system and the three-stage refrigeration system share the evaporative condenser 600 to form a double-machine cascade refrigeration system.
In the three-stage refrigeration system, a two-way defrosting system (a two-stage defrosting system) is led out from the outlet of the three-stage oil separator 502, the high-temperature refrigerant inlet of the defrosting branch III (defrosting 3) is connected with the fifth control valve 505 and the middle 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 middle pipeline of the first cryogenic heat exchanger 109 through the seventh control valve 507. The high-temperature refrigerant inlet of the fourth defrosting branch (defrosting 4) is connected with the sixth control valve 506 and the middle pipeline of the second cryogenic heat exchanger 110 through the fourth electromagnetic valve 904, and the low-temperature refrigerant outlet is connected with the fourth throttling element 504 and the middle pipeline of the second cryogenic heat exchanger 110 through the eighth control valve 508. The low-temperature refrigerant in the third defrosting branch is sent to the condensing side inlet of the evaporative condenser from the seventh control valve 507, the low-temperature refrigerant in the fourth defrosting branch is sent to the condensing side inlet of the evaporative condenser from the eighth control valve 508, and the switching control valve 510 is arranged between the refrigerant inlets of the two defrosting systems and the refrigerant outlets of the two defrosting systems.
According to the invention, the differential pressure value and the running time of the oil gas channel are measured through the differential pressure transmitter, the proper oil gas channel is selected, the continuity parameters of the device are ensured, for example, the differential pressure value is set to 20kPa, the running time is set to 12 hours, either one of the differential pressure value and the running time reaches the set value to indicate that the current channel is frozen and blocked, and the control system pre-cools 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 which is arranged between a first shallow-cooling heat exchanger 107 and a first deep-cooling heat exchanger 109, a second differential pressure transmitter 203 which is arranged between a second shallow Leng Huanre device 108 and a second deep-cooling heat exchanger 110, a three-way reversing valve 204 which is communicated with the outlets of the first deep-cooling heat exchanger 109 and the second deep-cooling heat exchanger 110 respectively, and a control element 205 (PLC) 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 interlocked, and the control element 205 organically integrates the oil gas system and the refrigeration system together, so that the automatic and reliable operation can be realized.
In the present 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 shut-off valves 700 adopting multiple seal protection, and are made of whole stainless steel materials. The first to eighth control valves are multiple-seal-protection zero-leakage pneumatic double-acting piston low-temperature cut-off valves and a meticulous control system, so that small temperature fluctuation in the switching process of the device is ensured.
In addition, as is common in the art, the primary refrigeration system may also be provided with a liquid receiver and a dry filter after the primary condenser 303; similarly, the secondary refrigeration system may also be provided with a liquid receiver and a dry filter after the secondary condenser 403; the three stage refrigeration system may also include a receiver and a dry filter after the evaporative condenser 600.
As shown in fig. 4 to 6, the low temperature cut-off valve 700 has the following 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 the outer periphery of the valve core element 703 is a valve cavity 706.
The valve body 701 has three sealing surfaces, two ends are respectively an inlet and an outlet of the valve body 701, the top is a connecting port, the sealing end surfaces of the inlet and the outlet of the valve body 701 are flange structures, and the flange structures in the embodiment are loose flange, so that the sealing performance is good, the corrosion resistance is high, and the maintenance and the installation are easy. The connection port of the valve body 701 is sealed by a valve seat 702, a valve cavity gasket 707, and a spool element 703, and the valve seat 702 is fixed to the spool element 703 by a second bolt 7021. The connecting port of the valve body 701 is a conventional static sealing surface, and no hidden trouble of leakage exists.
Specifically, a passage 7011 that is opened or closed by up-and-down movement of a valve seat 702 is provided between the inlet and outlet of the valve body 701 of the present invention. The valve seat 702 is provided with a mounting hole through which a bolt passes, 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 provided at the cylinder wall of the upper end face (connection port) of the valve body 701.
The spool member 703 includes a connecting rod 7031, a bellows joint 7032, a spool 7033 disposed at a lower end of the bellows joint 7032, and a sealing plate 7034 disposed at an upper end of the bellows joint 7032, wherein one end of the connecting rod 7031 is fixedly connected to the valve seat 702 by a second bolt 1021, and a top end of the connecting rod 7031 is fixed to the push rod 704. As shown in fig. 4 to 6, the inner diameter of the connection port 7012 between the valve element 7033 and the valve body 701 is equal to the inner diameter of the connection port, so that the connection port is sealed, and a valve cavity gasket 707 is provided at the connection between the valve element 7033 and the valve body 701, so that the sealing effect is enhanced, and leakage is prevented. The connecting rod 7031 is secured to the pushrod 704 through the spool 7033. In order to prevent part of refrigerant from entering the valve body 706 through a gap between the two parts when the connecting rod 7031 moves up and down, a section of bellows joint 7032 is arranged above the valve core 7033, the bellows joint 7032 is sleeved on the periphery of the connecting rod 7031, the bottom end of the bellows joint 7032 is fixedly sealed with the upper surface of the valve core 7033, the upper end of the valve core 7033 is fixedly sealed with a sealing plate 7034, so that the upward-flowing refrigerant enters a cavity formed between the bellows joint 7032 and the connecting rod 7031, the sealing plate 7034 is completely sealed with the connecting rod 7031, and the sealing plate 7034 moves up and down along with the connecting rod 7031, so that the refrigerant is prevented from leaking between the sealing plate 7034 and the connecting rod 7031. The seal plate 7034 serves to secure the bellows joint 7032 and seal. The outer diameter of the closure plate 7034 engages the inner wall of the valve cavity 706 and is movable up and down along the inner wall of the valve cavity 706. The bellows joint 7032 arranged on the valve element 703 has good elastic displacement and rigidity; when the valve is opened, medium refrigerant is in a cavity formed by the corrugated pipe joint 7032 and the connecting rod 7031, and the volume change caused by quenching and shock heating of the refrigerant automatically compensates and eliminates thermal stress through the corrugated pipe, so that leakage is avoided, and the service life of the valve is prolonged. The bottom end (lower end surface) of the valve cavity 706 arranged on the periphery of the valve core element 703 is in a flange structure, and a first bolt 1061 is fixed between the lower end surface of the valve cavity 706 and the sealing end surface of the valve body 701. The top end (upper end face) of the valve chamber 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 post 7062.
The cylinder 705 comprises a cylinder sleeve 7051, an upper cylinder cover 7052, a lower cylinder cover 7053, a first air source interface 7054, a second air source interface 7055 and a piston 7056, wherein the upper cylinder cover 7052 and the lower cylinder cover 7053 are arranged at the upper end and the lower end of the cylinder sleeve 7051, the first air source interface 7054 is arranged on the upper cylinder cover 7052, the second air source interface 7055 is arranged on the lower cylinder cover 7053, the piston 7056 is arranged in the cylinder sleeve 7051, 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 to the bottom end of the push rod 704 by a first nut 7066, and a dust ring 7063, a filler 7064 and an O-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 interface 7054, the first air source interface 7054 receives an input signal, instrument wind is introduced into the interface, pressure presses down the piston 7056, drives the push rod 704, the valve core element 703 and the valve seat 702, and enables the valve seat 702 to move to the limit position to close the switching valve; the lower cylinder cover 7053 is provided with a second air source interface 7055, the second air source interface 7055 receives an input signal, instrument air is introduced into the interface, pressure pushes up the piston 7056, drives the push rod 704, the valve core element 703 and the valve seat 702, and enables the valve seat 702 to be separated from a central channel of the valve body 701 to open the switching valve. The low-temperature switching valve can be used with an electromagnetic valve, and the low-temperature switching valve controls instrument wind 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 to respond.
The fluid medium passing through the switching valve is a refrigerant, the working temperature range of the switching valve is from minus 100 ℃ to 120 ℃, the working temperature can be instantaneously increased from the lowest point to the highest point and also can be reduced from the highest point to the lowest point, and the switching valve can bear the thermal stress change caused by quenching and quenching at minus 100 ℃ to 120 ℃ through the arrangement of the corrugated pipe joint, so that the stability of the piston type pneumatic low-temperature switching valve is improved; 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 is avoided strictly at the two inlet and outlet sides when the valve is closed, and meanwhile, the medium in the valve body leaks to the outside.
The oil tanker wharf oil gas recovery method is characterized in that under the condition that a channel A is smooth:
the high-temperature high-pressure refrigerant gas discharged by the first-stage refrigeration compressor 301 is separated by the first-stage oil separator 302 and then enters the first-stage condenser 303 to be condensed into high-pressure refrigerant liquid, the high-pressure refrigerant liquid is separated into two paths, the low-temperature low-pressure gas-liquid two-phase mixture is reduced in pressure by the pre-cooling throttling element 304 and the first throttling element 305 and enters the pre-cooling heat exchanger 106 and the first shallow-cooling heat exchanger 107 respectively, the low-temperature low-pressure gas-liquid two-phase mixture is evaporated in the pre-cooling heat exchanger 106 and the first shallow-cooling heat exchanger 107 and absorbs the heat of oil gas passing through the low-temperature low-pressure gas-liquid two-phase mixture, so that the oil gas passing 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 first-stage gas-liquid separator 311 and then enters the next cycle by the first-stage refrigeration compressor 301 after being fully vaporized;
the high-temperature and high-pressure refrigerant gas discharged by the secondary refrigeration compressor 401 is separated into oil by the secondary oil separator 402, then enters the secondary condenser 403 to be condensed into high-pressure refrigerant liquid, the high-pressure refrigerant liquid is absorbed by the gas-fluorine heat exchanger 112 to be cooled by the cold energy of low-temperature oil gas, the low-temperature and low-pressure gas-liquid two-phase mixture is reduced by the fifth throttling element 404, then enters the evaporation condenser 600, and is evaporated in the evaporation condensation heat exchanger 600 and absorbs the heat of the high-temperature and high-pressure refrigerant discharged by the third refrigeration compressor 501 (explosion-proof refrigeration compressor) in the evaporation condensation heat exchanger 600, so that the refrigerant flowing through the third-stage system is condensed, and the refrigerant is compressed by the secondary gas-liquid separator 405 again by the secondary refrigeration compressor 401 to enter the next cycle after being fully vaporized;
the high-temperature and high-pressure refrigerant gas discharged by the third refrigeration compressor 501 is separated into oil by the three-stage oil separator 502, then enters the evaporation and condensation heat exchanger 600 by the switching control valve 510 to be condensed into high-pressure supercooled refrigerant liquid, throttled and depressurized by the third throttling element 503 to be a low-temperature and low-pressure vapor-liquid two-phase mixture, enters the first cryogenic heat exchanger 109, and the low-temperature and low-pressure vapor-liquid two-phase mixture 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 passing 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 again by the three-stage gas-liquid separator 509 to enter the next cycle after being fully vaporized.
Under the condition of freezing and blocking of the B channel, the oil gas recovery of the oil tanker wharf is defrosted by the following method:
(S21) obtaining an instruction to be switched through a control system, separating out part of refrigerant (1/7-1/5 refrigerant) to the standby oil-gas channel in advance, and switching after the standby 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 separated by the primary oil separator 302 and then enters the second shallow Leng Huanre device 108 through the second electromagnetic valve 902, and solid oil attached to the surface of a heat exchange tube in the second shallow Leng Huanre device 108 absorbs heat of the refrigerant to defrost, so that the second shallow Leng Huanre device 108 absorbs heat to defrost again for later use, and is condensed into high-pressure refrigerant liquid to be combined with condensate of the primary condenser 303 through the fourth control valve 310 and then enters the system for circulation.
The high-temperature high-pressure refrigerant gas discharged by the third refrigeration compressor 501 during the operation of the secondary defrosting system is separated into oil by the secondary oil separator 502, then enters the second cryogenic heat exchanger 110 through the fourth electromagnetic valve 904, and is adhered to the surface solid oil of the heat exchange tube in the second cryogenic heat exchanger 110 to absorb the heat of the refrigerant so as to defrost, so that the second cryogenic heat exchanger 110 absorbs the heat to defrost again for later use, is condensed into high-pressure refrigerant liquid, is connected into the evaporative condensing heat exchanger 600 through the eighth control valve 508, and then enters the system circulation.
Similarly, under the condition of freezing and blocking the channel A, defrosting is carried out on the channel A by controlling the defrosting branch I and the defrosting branch III, and the rest working methods are the same as those of the channel B.
The liquid oil which is condensed out is led to the oil collecting tank from the bottom oil outlet, and the low-concentration oil gas can be discharged directly after reaching the standard or enter the next link, such as: the adsorption section and the oxidation catalysis section are used for further purification treatment.
Example 2: the throughput was 300m 3 Oil gas recovery device for/h oil tanker wharfThe oil gas is volatile oil gas of the finished oil, and the inlet air concentration is 1000g/m 3 The wharf oil gas recovery device in the current market is formed by combining two sets of-70 ℃ single-way condensation oil gas recovery systems, the power of an air pump is 5.5kW, the power of the single-way condensation system is 49.4kW, the total unit power is 104.3kW, and the unit energy consumption is 0.348 kW/(m) 3 /h)。
300m of the invention 3 The final oil gas temperature of the oil wheel wharf oil gas recovery device is-70 ℃, the air pump is the Shandong Feng source explosion-proof Roots air pump power of 5.5kW, the first-stage explosion-proof compressor of the two-way condensing system is the German Bitzer piston compressor 4GE-23Y, the power of 14.3kW, the second-stage explosion-proof compressor is the Taiwan Fusheng screw compressor CSR170-Ex of China, the power of 34.6kW, the third-stage explosion-proof compressor is the German Bitzer piston compressor 6HE-28Y, the power of 12.4kW, the explosion-proof axial fan for the air cooling heat exchanger is Suzhou Rui wave, the power of 4.0kW, the total unit power is 70.8kW, and the unit energy consumption is 0.236 kW/(m) 3 And/h), the energy efficiency is improved by 47.5 percent.
As described above, although the oil and gas recovery apparatus for a tanker terminal of the present invention has been shown and described with reference to specific preferred embodiments, it is within the scope of the present invention not limited to the purely condensation type oil and gas recovery apparatus, but may be changed to a combination of condensation+adsorption, oxidation catalytic function, etc. 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 (7)
1. The oil and gas recovery method for the oil tanker wharf is characterized by comprising the following steps of:
(S1) the oil gas to be treated fed from the oil gas inlet is fed into an oil gas system, sequentially passes through a regenerative heat exchanger, a precooling heat exchanger, a shallow Leng Huanre device, a cryogenic heat exchanger and a gas fluorine heat exchanger in the oil gas system, liquefies the oil gas through heat exchange with a refrigerant fed out of a refrigerating system, and feeds the oil gas treated by the gas fluorine heat exchanger into the regenerative heat exchanger again, exchanges heat in the regenerative heat exchanger and is discharged;
(S2) the refrigeration system comprises a primary refrigeration system, a secondary refrigeration system and a tertiary refrigeration system; the primary refrigeration system sends the refrigerant into a pre-cooling heat exchanger and a shallow Leng Huanre device to exchange heat with oil gas; the second-stage refrigerating 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 evaporation condenser; the three-stage refrigerating system sends the refrigerant into a cryogenic heat exchanger to exchange heat with oil gas, and the refrigerant after heat exchange returns to a refrigerating compressor of the three-stage refrigerating system to perform refrigerating cycle;
(S3) when the system needs defrosting, the high-temperature and high-pressure refrigerant sent out from the primary refrigeration system is sent into the shallow cooling heat exchanger for defrosting, and the high-temperature and high-pressure refrigerant sent out from the tertiary refrigeration system is sent into the deep cooling heat exchanger for defrosting;
the shallow cooling heat exchanger comprises a first shallow cooling heat exchanger and a second shallow Leng Huanre device which are 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 primary refrigeration system comprises a primary refrigeration compressor and a primary condenser connected with a refrigerant outlet of the primary refrigeration compressor, and an outlet of the primary condenser is respectively connected with inlets of the pre-cooling heat exchanger, the first shallow-cooling heat exchanger and the second shallow-cooling heat exchanger; the secondary refrigeration system comprises a secondary refrigeration compressor, a secondary condenser and an evaporation condenser, wherein the secondary condenser is connected with an outlet of the secondary refrigeration compressor; the outlet of the secondary condenser is connected with the refrigerant inlet of the gas-fluorine heat exchanger, and the evaporation side inlet of the evaporation condenser is connected with the outlet of the gas-fluorine heat exchanger; the three-stage refrigeration system comprises a three-stage refrigeration compressor and an evaporation condenser connected with the three-stage refrigeration compressor; the condensing side outlet of the evaporative condenser is connected with the inlets of the first cryogenic heat exchanger and the second cryogenic heat exchanger respectively;
two paths of defrosting branches are led out from the outlet of the primary refrigeration compressor and are connected with the first shallow cooling heat exchanger and the second shallow cooling heat exchanger respectively; two paths of defrosting branches are respectively led out from a condensing side inlet of the evaporative condenser and are connected with the first cryogenic heat exchanger and the second cryogenic heat exchanger;
the first shallow cooling heat exchanger and the second shallow Leng Huanre device of the primary refrigeration system are controlled by the primary refrigeration compressor, so that alternating refrigeration, temperature reduction, heating and defrosting can be realized;
the first cryogenic heat exchanger and the second cryogenic heat exchanger of the three-stage refrigeration system are controlled by the three-stage refrigeration compressor, and can alternately refrigerate, heat and defrost.
2. The oil and gas recovery method of a tanker terminal according to claim 1, wherein the refrigerant sent out of two defrosting branches led out from the outlet of the primary refrigeration compressor is merged with the refrigerant sent out from the outlet of the primary condenser; and the two defrosting branches led out from the inlet of the condensing side of the evaporative condenser are used for merging the refrigerant after heat exchange with the refrigerant sent into the evaporative condenser again.
3. The oil and gas recovery method of the tanker wharf according to claim 2, wherein a switching control valve is provided between the inlets of the two defrosting branches led out from the condensation side of the evaporative condenser and the outlets of the two defrosting branches.
4. The oil and gas recovery method of the tanker dock according to claim 3, wherein the inlet of the pre-cooling heat exchanger is provided with a pre-cooling throttling element, the inlet of the first shallow cooling heat exchanger is provided with a first throttling element, and the inlet of the second shallow cooling heat exchanger is provided with a second throttling element; a third throttling element is arranged between the condensing side outlet of the evaporative condenser and the inlet of the first cryogenic heat exchanger, and a fourth throttling element is arranged between the condensing side outlet 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 inlet of the evaporation side of the evaporation condenser.
5. The oil and gas recovery method of the tanker dock according to claim 1, wherein a first control valve is arranged between an outlet of the primary compressor and the first shallow-cooled heat exchanger, and a second control valve is arranged between an outlet of the primary compressor and the second shallow-cooled 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 condensing side inlet of the evaporative condenser and the first cryogenic heat exchanger, and a sixth control valve is arranged between the condensing 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.
6. The tanker terminal hydrocarbon recovery method according to claim 1, wherein the hydrocarbon system is provided with a control system comprising a pressure transmitter and a shut-off valve provided at a hydrocarbon inlet.
7. The oil and gas recovery method of a tanker dock according to claim 1, wherein a first differential pressure transmitter is arranged between the first shallow-cooled heat exchanger and the first cryogenic heat exchanger; a second differential pressure transmitter is arranged between the second shallow Leng Huanre device and the second cryogenic heat exchanger.
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