CN215916499U - Oil gas recovery device with adjustable treatment capacity for multistage condensation, adsorption and cabin return - Google Patents
Oil gas recovery device with adjustable treatment capacity for multistage condensation, adsorption and cabin return Download PDFInfo
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- CN215916499U CN215916499U CN202120531510.7U CN202120531510U CN215916499U CN 215916499 U CN215916499 U CN 215916499U CN 202120531510 U CN202120531510 U CN 202120531510U CN 215916499 U CN215916499 U CN 215916499U
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Abstract
The utility model discloses an oil gas recovery device with adjustable processing capacity of multistage condensation, adsorption and cabin return, which comprises a precooling heat exchanger, a desulfurizing tower, a buffer tank, a multistage condensation unit, an adsorption device and an oil-water separation device, wherein the multistage condensation unit comprises a first-stage refrigerating unit and a cryogenic unit, the adsorption device comprises two adsorption tanks and a vacuum pump which are connected in parallel, and the oil-water separation device comprises an oil-water separator and an oil storage tank.
Description
Technical Field
The utility model belongs to the technical field of wharf and ship waste gas treatment, and particularly relates to an oil gas recovery device with adjustable treatment capacity of multistage condensation, adsorption and cabin return.
Background
The rapid development of the transportation of the ship oil cargo greatly meets the development requirements of the economic society, but also brings Volatile Organic pollutants (VOC) of oil gas, and the Volatile Organic Compounds of oil gas pollute the atmosphere. The international maritime organization approved in 1997 that rules for preventing atmospheric pollution from ships were added to the MARPOL73/78 antifouling convention, and implemented in force in 2005; various countries in the world also take a series of countermeasures for preventing atmospheric pollution caused by ship oil gas. The state governments along the united states required port tankers to use oil and gas recovery systems since 1998 and to be equipped with VOC receivers in each loading and unloading ship port in succession; in european areas, many countries have oil and gas recovery processing units installed at oil tanker terminals, and some shuttle tankers have also installed ship oil and gas recovery units. The international maritime organization IMO also passed the VOC management planning guidelines on the 59 th maritime environmental protection agency mepc.185(59) in 2009 and was executed from 7/1/2010, specifying that "oil transport vessels must be provided with a tanker cargo tank VOC collection piping and safely transported to the piping of the terminal oil and gas recovery device", thereby strengthening the management work on the control of the tanker VOC emissions.
The ship transportation of crude oil is the most important transportation mode of crude oil import in China, and the crude oil generates high-concentration and large-treatment-capacity oil and gas emission in transportation and wharf ship loading operation, so that huge economic loss is caused, environmental pollution is caused in oceans and areas around the wharf, and potential safety hazards are brought to production and life. The MARPOL73/78 convention rule VI takes effect in China, and starts the strengthening management of China in the aspect of oil and gas emission. The convention stipulates that an oil product transportation ship must be provided with an oil cargo tank oil gas VOC collection pipe system and a pipe system safely conveyed to an oil gas recovery device at a wharf, but the convention has no specific limiting indexes aiming at the oil gas emission of the ship.
As the oil gas recovery device in port and wharf is gaining attention, the application of the oil gas recovery device in the crude oil transportation vessel will become necessary and urgent, and the oil gas recovery device will become an indispensable matching device on the crude oil transportation vessel. The utility model provides an oil gas recovery device with adjustable multistage condensation, adsorption and back-to-cabin treatment capacity, which is mainly used for solving the problem that the development of an oil gas recovery system of a crude oil transportation ship, which has independent intellectual property rights, is mature, reliable, safe and efficient, is important in the aspects of mandatory constraint of rules at home and abroad and the realistic requirements of safety, environmental protection and energy conservation in China.
SUMMERY OF THE UTILITY MODEL
In view of the above problems, the main objective of the present invention is to design an oil gas recovery device with adjustable throughput for multi-stage condensation, adsorption and tank return, which solves the problem of oil gas emission with high concentration and large throughput during the transportation and loading operation of the wharf, reduces the problem of huge economic loss caused by oil gas emission, reduces the pollution problem of the environment around the ocean and the wharf, and reduces the potential safety hazard brought to production and life by oil gas emission.
In order to achieve the purpose, the utility model adopts the following technical scheme:
a multi-stage condensation + adsorption + return cabin treatment capacity adjustable oil gas recovery device comprises a precooling heat exchanger, a desulfurizing tower, a buffer tank, a multi-stage condensation unit, an adsorption device and an oil-water separation device;
the oil-water separation device comprises an oil-water separator and an oil storage tank, wherein the oil-water separator is provided with an inlet, an outlet and a sewage draining outlet, the outlet of the oil-water separator is connected with the oil storage tank, and an explosion-proof oil pump and an oil storage place are arranged below the oil storage tank;
the front part of the desulfurizing tower is provided with a cooling medium inlet and a cooling medium outlet, a liquid outlet is arranged below the desulfurizing tower and is connected to the oil-water separator;
the multistage condensing unit comprises a primary refrigerating unit and a cryogenic unit, wherein a 2-8 ℃ cold box is arranged in the primary refrigerating unit, two cold boxes are arranged in the cryogenic unit, the 2-8 ℃ cold box is connected to the cold box of the cryogenic unit, and a lower liquid outlet of the 2-8 ℃ cold box is connected to an inlet of the oil-water separator;
the front parts of the primary refrigerating unit and the cryogenic unit are both provided with a cooling medium inlet and a cooling medium outlet, two flame arresters and a fan are arranged between the cryogenic unit and the primary refrigerating unit, and the fan is arranged between the two flame arresters;
the adsorption device comprises two adsorption tanks and a vacuum pump which are connected in parallel, a flame arrester is arranged at the front and the rear of the vacuum pump, the vacuum pump is respectively connected with a water condenser, an air condenser and a water tank, the air condenser, the water tank and the water condenser are mutually connected, and a cooling water pump is arranged on the water tank;
the adsorption tank is provided with an emptying pipeline and a cabin returning pipeline;
the precooling heat exchanger is provided with two air inlets and two air outlets, the front part of one air inlet is provided with an oil-gas inlet, the oil-gas inlet is provided with a flame arrester, the other air inlet is connected with the deep cooling unit, one air outlet is connected with the desulfurizing tower, and the other air outlet is connected with the adsorption device;
the buffer tank is provided with three air inlets and an air outlet, the air outlet is connected with a 2-8 ℃ cold box, one air inlet is connected with the desulfurizing tower, one air inlet is connected with a water condenser of the adsorption device, and the other air inlet is connected with the oil-water separation device.
As further description of the utility model, the oil-water separator and the adsorption tank are both provided with nitrogen pipes, and the nitrogen pipes are provided with pressure stabilizing valves.
As a further description of the utility model, the adsorption device comprises two adsorption tanks which are alternately used for adsorption and desorption, and when one adsorption tank is used, the other adsorption tank is used as a desorption tank.
As a further description of the utility model, a cooling water coil is arranged in the desulfurizing tower, and the desulfurizing agent in the desulfurizing tower is ferric oxide.
As a further description of the utility model, the storage location comprises a sump on a ship.
As further description of the utility model, the cold box of the cryogenic unit comprises two to ten stages of coolers, and the condensation temperature of each stage is reduced by 10-30 ℃ until the outlet temperature of the cold box is lower than-170 ℃.
As further description of the utility model, the last stage cooler of the cold box of the deep cooling unit is set as a cascade compressor unit, the cascade stage number is greater than two stages, and oil gas in the cold boxes of two to nine stages and oil gas at the outlet of the last stage perform countercurrent heat exchange.
As further description of the utility model, fire arresters are arranged on the emptying pipeline and the cabin returning pipeline.
Compared with the prior art, the utility model has the technical effects that:
the utility model provides an oil gas recovery device with adjustable processing capacity of multistage condensation, adsorption and cabin return, wherein liquid substances in a multistage condensation unit are collected in a cold box, an adsorption tank is matched with a vacuum pump, adsorbed oil gas is pumped into a buffer tank through the vacuum pump, condensation recovery processing is carried out again, the oil gas is directly emptied through processing of the adsorption device or enters the cabin again as inert gas, the cryogenic unit adopts one standby system, and a set of standby systems are alternately used when ice blocks frost.
Drawings
Fig. 1 is an overall view of the present invention.
In the figure, 1, a precooling heat exchanger, 2, a desulfurizing tower, 3, a buffer tank, 4, a multi-stage condensing unit, 41, a first-stage refrigerating unit, 42, a cryogenic unit, 5, an adsorption device, 51, an adsorption tank, 52, a vacuum pump, 53, a water condenser, 54, an air condenser, 55, a water tank, 6, an oil-water separation device, 61, an oil-water separator and 62, an oil storage tank.
Detailed Description
The utility model is described in detail below with reference to the attached drawing figures:
the utility model provides a throughput adjustable oil gas recovery unit of multistage condensation + absorption + back cabin, refers to fig. 1 and shows, includes precooling heat exchanger 1, desulfurizing tower 2, buffer tank 3, multistage condensation unit 4, adsorption equipment 5 and oil water separator 6.
The oil-water separation device 6 comprises an oil-water separator 61 and an oil storage tank 62, an inlet, an outlet and a sewage draining port are formed in the oil-water separator 61, the outlet of the oil-water separator 61 is connected with the oil storage tank 62, an anti-explosion oil pump and an oil storage place are arranged below the oil storage tank 62, and the oil storage place comprises a dirty oil tank on a ship.
The front part of the desulfurizing tower 2 is provided with a cooling medium inlet and a cooling medium outlet, a liquid outlet is arranged below the desulfurizing tower 2, and the liquid outlet is connected to the oil-water separator 61.
The front portions of the first-stage refrigerating unit 41 and the cryogenic unit 42 are both provided with a cooling medium inlet and a cooling medium outlet, two flame arresters and a fan are arranged between the cryogenic unit 42 and the first-stage refrigerating unit 41, the fan is arranged between the two flame arresters, and the fan is arranged as a variable-frequency fan.
The adsorption device 5 comprises two adsorption tanks 51 and a vacuum pump 52 which are connected in parallel, a flame arrester is arranged at the front and the rear of the vacuum pump 52, the vacuum pump 52 is respectively connected with a water condenser 53, an air condenser 54 and a water tank 55, the air condenser 54, the water tank 55 and the water condenser 53 are mutually connected, and a cooling water pump is arranged on the water tank 55.
The adsorption tank 51 is provided with an emptying pipeline and a return cabin pipeline, fire arresters are arranged on the emptying pipeline and the return cabin pipeline, an emptying valve is arranged on the emptying pipeline, and a return cabin valve is arranged on the return cabin pipeline.
In the adsorption device 5, two adsorption tanks 51 alternately perform adsorption and desorption, and when one adsorption tank is used, the other adsorption tank is used as a desorption tank.
Precooling heat exchanger 1 on set up two air inlets and two gas outlets, the front portion of an air inlet sets up the oil gas import, sets up spark arrester and admission valve in the oil gas import, another air inlet is connected with cryrogenic unit 42, a gas outlet is connected with desulfurizing tower 2, another gas outlet is connected with adsorption equipment 5.
The buffer tank 3 is provided with three air inlets and an air outlet, the air outlet is connected with a 2-8 ℃ cold box, one air inlet is connected with the desulfurizing tower 2, one air inlet is connected with the water condenser 53 of the adsorption device 5, and the other air inlet is connected with the oil-water separation device 6.
And nitrogen pipes are arranged on the oil-water separator 6 and the adsorption tank 51, pressure stabilizing valves are arranged on the nitrogen pipes, when the equipment stops running, the pressure stabilizing valves are opened to introduce nitrogen into the nitrogen pipes, and residual oil gas can be replaced through the introduction of the nitrogen.
The desulfurizing tower 2 is internally provided with a cooling water coil pipe, and a desulfurizing agent in the desulfurizing tower 2 is ferric oxide, wherein the ferric oxide desulfurizing agent is a high-efficiency gas purifying agent which is processed by taking ferric oxide as a main active component and adding other promoters.
The cold box of the deep cooling unit 42 comprises two to ten stages of coolers, the condensing temperature of each stage is reduced by 10-30 ℃ until the outlet temperature of the cold box is lower than-170 ℃, the last stage of cooler is set to be a cascade compressor unit, the cascade stage number is greater than two stages, and oil gas in the two to nine stages of cold boxes is subjected to countercurrent heat exchange with the outlet oil gas of the last stage.
It should be noted that the specific operation logic of each part of the present invention is as follows:
the oil gas inlet pipeline of the utility model is provided with a flow transmitter, a pressure transmitter and a temperature transmitter, and the pressure of the cargo hold, the flow rate of oil gas and the temperature of oil gas are monitored at an oil gas outlet (the flow transmitter, the pressure transmitter and the temperature transmitter are arranged in front of a flame arrester):
when the pressure of the cargo hold is higher than 12kPa, the multistage condensing unit 4 is started in a chain manner to build a cold field;
when the pressure of the cargo compartment is higher than 13kPa, opening an air inlet valve on an oil gas inlet, and starting a fan;
and when the pressure of the cargo hold is lower than 11kPa, the multistage condensing unit 4, the air inlet valve, the fan and the compartment returning valve are closed in sequence.
When the temperature of the oil gas is higher than 85 ℃, the system gives out a high-temperature alarm;
when the temperature of the oil gas is higher than 88 ℃, the system sends out a high-temperature alarm, closes the air inlet valve and shuts down the fan and the compressor unit of the deep cooling unit 42.
The flow transmitter arranged on the oil gas inlet pipeline is interlocked with the fan to control the air quantity of the fan, so that the flow of oil gas entering the oil gas recovery device disclosed by the utility model is ensured to be adjustable.
The system is characterized in that a total hydrocarbon sensor and an oxygen content sensor are arranged on the oil gas inlet pipeline, the total hydrocarbon sensor and the oxygen content sensor are arranged behind the flame arrester, when the oxygen content in oil gas exceeds 6%, the system sends out an oxygen content alarm, when the oxygen content in oil gas exceeds 8%, the system sends out an oxygen content high alarm, an air inlet valve of an oil gas inlet is closed, and the fan and the compressor unit are shut down.
The oil gas enters a desulfurizing tower 2 after passing through a precooling heat exchanger 1, and when the temperature of the oil gas is higher than 65 ℃, the system sends out a high-temperature alarm; when the temperature of the oil gas is higher than 85 ℃, the system sends out a high-temperature alarm, closes the air inlet valve and shuts down the fan and the compressor unit.
The desulfurized oil gas passes through the buffer tank, enters a 2-8 ℃ cold box of the primary refrigerating unit after being buffered, a temperature transmitter is arranged at an outlet of the 2-8 ℃ cold box, the temperature transmitter and the 2-8 ℃ cold box run in a linkage mode, the compressor unit is started when the temperature of the oil gas is higher than 8 ℃, and the compressor unit is closed when the temperature of the oil gas is lower than 2 ℃.
The cold box of deep cooling unit 42 is multistage overlapping compressor unit, and two cold boxes are the cold box group of establishing ties, and the cold box is one and one to be equipped with, sets up automatic valve before every cold box, but automatic valve automatic switch, compressor unit only acts on last one-level cold box, and the system monitors the exit differential pressure of cold box group (the import department of cold box sets up differential pressure transmitter):
when the differential pressure is larger than 3kPa, the compressor unit introduces a refrigerant to the standby cold box set to establish a cold field;
when the differential pressure is greater than 5kPa, the automatic valve rotates, the cold box set is switched, and the cold box set which stops working is defrosted;
the pipe side and shell side gas outlets of each stage of cold box of the deep cooling unit 4 are respectively provided with a temperature transmitter to monitor the working condition of the condensing unit.
The oil gas flowing out of the deep cooling unit 42 exchanges heat with the oil gas at the main inlet and then is divided into two branches, one branch enters the adsorption device 5, and the other branch returns to the cargo hold or is emptied:
when the pressure of the cargo hold is lower than 11kPa, the oil gas directly returns to the cargo hold through a cargo returning pipeline;
when the pressure of the cargo hold is higher than 11kPa and the concentration of the non-methane total hydrocarbons is lower than 5g/m during the cultivation, directly emptying the oil gas through an emptying pipeline;
when cargo hold pressure is above 11kPa while the non-methane total hydrocarbon concentration is greater than 5g/m, the oil and gas enter the adsorption unit.
Be equipped with temperature transmitter on the adsorption tank 51, when the oil gas temperature is higher than 50 ℃, send high temperature alarm, when the oil gas temperature is higher than 65 ℃, send high temperature alarm to close the admission valve that sets up on adsorption equipment 5 simultaneously, open the blowoff valve, start vacuum pump 52 and carry out the desorption to adsorption tank 51, cooling water pump, fan and vacuum pump 51 interlocking start, stop, cooling water pump, fan start earlier than vacuum pump 30s promptly, cooling water pump, fan shut down after 30 s.
The oil and water condensed by the cold box are collected to an oil-water separator 61, sewage is automatically discharged to a treatment place through a sewage discharge outlet, liquid hydrocarbons flow to an oil storage tank, and when the liquid level reaches a high level value, an explosion-proof oil pump is started; and when the liquid level reaches a low level value, the explosion-proof oil pump is closed.
The cold box (refrigeration heat exchanger unit) of the cryogenic unit 42 describes:
1. the method comprises the following steps of setting sectional condensation description for a cold box of a deep cooling unit:
the multi-stage condensation and heat exchange process is the last stage of-170 ℃, and the waste gas condensed by the deep cooling unit 42 flows back to the front waste gas for cooling and heat exchange.
The first stage is a water removal stage, the temperature is 2-8 ℃, about 68% of water in air is condensed and recovered, the second stage is a shallow condenser, the condensation temperature is about-20 to-30 ℃, a small part of oil-gas mixed liquid in waste gas is condensed and recovered, the third stage is a low-temperature condenser, the condensation temperature is about-50 to-60 ℃, a medium part of oil-gas mixed liquid in waste gas is condensed and recovered, the fourth stage is a deep cooling condenser, the condensation temperature is about-70 to-80 ℃, most of oil-gas mixed liquid in waste gas is condensed, in the same way, the condensation temperature of each stage is reduced by 10-30 ℃, the condensation temperature of each stage is reduced to-170 ℃ after two to ten stages of condensation, and the condensed-170 ℃ waste gas flows backwards again to be regenerated by utilizing waste heat.
2. The dual-channel alternate switching use description:
the multistage condensing unit 4 adopts one for one and one spare, when a set of spare cold boxes are used as ice plugs and frost, the spare cold boxes are alternately used, the waste gas circulation is automatically switched to the spare cold boxes, the automatic valve at the front part of the cold boxes is automatically switched to enter the unit for defrosting, and the front-back pressure difference or the running time of the cold boxes are (alternatively, defrosting is executed as long as one item is met).
3. Temperature fluctuation control description in the double-channel switching process:
when the double-channel system operates, one group of cold boxes perform cooling and heat exchange, and the other group of cold boxes perform internal circulation cooling, so that the inside of the standby cold box can be maintained in a low-temperature state.
When the cold box that realizes the cooling heat transfer frosts, the stifled hot freon of needs of ice defrosting, and the system valve is automatic to carry out the condensation heat transfer with waste gas heat conduction standby system, and whole switching process can not cause the temperature fluctuation basically, and the cold box hot freon of cooling heat transfer washes the frost and finishes, carries out the inner loop cooling precooling once more, can maintain standby cold box inside and be in the low temperature state, and the circulation is reciprocal like this, repeats above flow.
The specific working process of the oil gas recovery device disclosed by the utility model is as follows:
monitoring the flow, pressure and temperature of the oil gas overflowing from the cargo hold, feeding the oil gas meeting the above-mentioned disclosure requirements into a precooling heat exchanger 1, passing through the tube side of the precooling heat exchanger 1, exchanging heat with the oil gas discharged by a copious cooling unit 42 in the precooling heat exchanger 1, feeding the oil gas into a desulfurizing tower 2, treating by a desulfurizing agent in the desulfurizing tower 2, and removing H2S (iron oxide desulfurizer 20 ℃; E)The catalyst has high removal performance on hydrogen sulfide at 100 ℃, has certain removal effect on thiol organic sulfur and most of nitrogen oxides, has the characteristics of simple equipment, convenient operation, high purification degree, small bed resistance, strong adaptability, no secondary pollution and the like in use, and can remove the hydrogen sulfide at high precision even under the severe conditions of no oxygen, no ammonia and the like).
In order to prevent the risk of high temperature of the desulfurizer, a cooling coil is arranged in the desulfurizing tower 2, and the amount of cooling water is 5-10 m3And simultaneously, a temperature transmitter is arranged on the desulfurizing tower 2, thermometers are arranged at a cold medium inlet and a cold medium outlet in front of the desulfurizing tower 2, and the thermometers and the temperature transmitter are used for monitoring the temperature of the oil gas in real time.
The oil gas after desulfurization enters the buffer tank 3, the fluctuation of the oil gas flow can be reduced by the buffer tank 3, and meanwhile, the oil gas is also a gathering position of overflow gas of the oil storage tank and desorption gas of the adsorption device 5.
The oil gas buffered by the buffer tank 3 enters a first-stage refrigerating unit 41, the condensation of the oil gas at the first stage mainly comprises removing water, condensing to 2-8 ℃, removing most of water in the oil gas, then the oil gas enters a deep cooling unit 42, the deep cooling unit 42 is an independent skid block, the deep cooling unit 42 adopts one use and one spare, when a set of spare cold boxes are used as ice blocks and frost, the spare cold boxes are alternately used, the outlet of the cold boxes is provided with flow detection, when the abnormal flow (lower than the set flow detected by a PLC or no flow) is detected, the alarm flow of the deep cooling unit 42 is abnormal, an automatic valve of the deep cooling unit 42 is automatically opened, waste gas circulating air is automatically switched to the spare cold boxes, the automatic valve is automatically switched to enter the cold boxes for defrosting, the qualified oil gas outlet of the deep cooling unit 42 is provided with a waste gas heat regeneration function, when the deep cooling unit 42 detects the conditions of blocking, icing and the like of the unit, the heating function is started, the oil gas discharged by the unit is sent to a heating system, heating to 40-60 ℃, re-entering a cryogenic unit for circulation to defrost, wherein waste gas is subjected to heat exchange by adopting a high-pressure refrigerant of a first compressor, heating the waste gas to 50 ℃, a cold box of the cryogenic unit 42 is composed of two to ten stages of coolers, the condensation temperature of each stage is reduced by 10-30 ℃ until the outlet temperature of oil gas is lower than-170 ℃, only the last stage of cooler is subjected to oil gas cooling by adopting a cascade compressor unit, the cascade stage number is greater than two, and the oil gas in the rest stages of cold boxes is subjected to heat exchange with the oil gas (containing residual cold) at the outlet of the last stage.
Therefore, the oil gas cold energy can be fully utilized, the energy consumption of the system is saved, the last stage of the deep cooling unit 42 can ensure that the temperature of the oil gas outlet is lower than-170 ℃, so that more than 90% of the oil gas can be removed, the temperature of the waste gas is about 0 ℃, and the oil gas exchanges heat with the imported high-temperature oil gas before entering the adsorption device 5, so that the oil gas can meet the temperature use requirement of the desulfurizing tower 2, and the energy consumption of the system can be saved.
After the oil gas enters the adsorption device 5, hydrocarbon in the tail gas is further adsorbed by a carbon molecular sieve, the adsorption device 5 comprises two adsorption tanks 51 and a vacuum pump 52, the vacuum pump 52 is adopted for desorption, the desorbed oil gas from the vacuum pump 52 is sent to an oil gas inlet of a condensation recovery section so as to condense and recover oil content in the oil gas, a desorption system of the vacuum pump 52 is provided with cooling water and an air cooling device (the cooling water from a water tank 55 is divided into two paths, one path enters the vacuum pump 52 and is used as cooling water of the vacuum pump 52, the other path enters a water condenser 53 for cooling the oil gas desorbed from the vacuum pump 52, the two paths of cooling water are converged and enter an air condenser 54, the temperature of the heated cooling water is reduced to the ambient temperature by air in the environment and then returns to the water tank 55 for recycling, the tail gas treated by the adsorption device 5 is selectively evacuated or returned to the cargo compartment according to the pressure condition of the cargo compartment, namely, the pressure of the cargo hold is lower than the set pressure, the tail gas returns to the cargo hold through a back-to-cargo-hold pipeline, the pressure of the cargo hold is higher than the set pressure, and the tail gas is emptied through an emptying pipeline.
The above embodiments are only for illustrating the technical solutions of the present invention and are not limited, and other modifications or equivalent substitutions made by the technical solutions of the present invention by the ordinary skilled person in the art are included in the scope of the claims of the present invention without departing from the spirit and scope of the technical solutions of the present invention.
Claims (8)
1. The utility model provides a multistage condensation + adsorb + return handling capacity adjustable vapor recovery system in cabin which characterized in that: the system comprises a precooling heat exchanger, a desulfurizing tower, a buffer tank, a multi-stage condensing unit, an adsorption device and an oil-water separation device;
the oil-water separation device comprises an oil-water separator and an oil storage tank, wherein the oil-water separator is provided with an inlet, an outlet and a sewage draining outlet, the outlet of the oil-water separator is connected with the oil storage tank, and an explosion-proof oil pump and an oil storage place are arranged below the oil storage tank;
the front part of the desulfurizing tower is provided with a cooling medium inlet and a cooling medium outlet, a liquid outlet is arranged below the desulfurizing tower and is connected to the oil-water separator;
the multistage condensing unit comprises a primary refrigerating unit and a cryogenic unit, wherein a 2-8 ℃ cold box is arranged in the primary refrigerating unit, two cold boxes are arranged in the cryogenic unit, the 2-8 ℃ cold box is connected to the cold box of the cryogenic unit, and a lower liquid outlet of the 2-8 ℃ cold box is connected to an inlet of the oil-water separator;
the front parts of the primary refrigerating unit and the cryogenic unit are both provided with a cooling medium inlet and a cooling medium outlet, two flame arresters and a fan are arranged between the cryogenic unit and the primary refrigerating unit, and the fan is arranged between the two flame arresters;
the adsorption device comprises two adsorption tanks and a vacuum pump which are connected in parallel, a flame arrester is arranged at the front and the rear of the vacuum pump, the vacuum pump is respectively connected with a water condenser, an air condenser and a water tank, the air condenser, the water tank and the water condenser are mutually connected, and a cooling water pump is arranged on the water tank;
the adsorption tank is provided with an emptying pipeline and a cabin returning pipeline;
the precooling heat exchanger is provided with two air inlets and two air outlets, the front part of one air inlet is provided with an oil-gas inlet, the oil-gas inlet is provided with a flame arrester, the other air inlet is connected with the deep cooling unit, one air outlet is connected with the desulfurizing tower, and the other air outlet is connected with the adsorption device;
the buffer tank is provided with three air inlets and an air outlet, the air outlet is connected with a 2-8 ℃ cold box, one air inlet is connected with the desulfurizing tower, one air inlet is connected with a water condenser of the adsorption device, and the other air inlet is connected with the oil-water separation device.
2. The oil gas recovery device with adjustable multi-stage condensation, adsorption and back-cabin treatment capacity of claim 1, characterized in that: and the oil-water separator and the adsorption tank are both provided with nitrogen pipes, and the nitrogen pipes are provided with pressure stabilizing valves.
3. The oil gas recovery device with adjustable multi-stage condensation, adsorption and back-cabin treatment capacity of claim 1, characterized in that: the adsorption device is characterized in that two adsorption tanks alternately adsorb and desorb, and when one adsorption tank is used, the other adsorption tank is used as a desorption tank.
4. The oil gas recovery device with adjustable multi-stage condensation, adsorption and back-cabin treatment capacity of claim 1, characterized in that: the inside of the desulfurizing tower is provided with a cooling water coil pipe, and a desulfurizing agent in the desulfurizing tower is ferric oxide.
5. The oil gas recovery device with adjustable multi-stage condensation, adsorption and back-cabin treatment capacity of claim 1, characterized in that: the oil storage place comprises a dirty oil tank on a ship.
6. The oil gas recovery device with adjustable multi-stage condensation, adsorption and back-cabin treatment capacity of claim 1, characterized in that: the cooling box of the deep cooling unit comprises two to ten stages of coolers, and the condensation temperature of each stage is reduced by 10-30 ℃ until the outlet temperature of the cooling box is lower than-170 ℃.
7. The oil gas recovery device with adjustable multi-stage condensation, adsorption and back-cabin treatment capacity of claim 6, wherein: the last cooler of the cold box of the deep cooling unit is set as a cascade compressor unit, the cascade stage number is greater than the second stage, and oil gas in the cold boxes of two to nine stages and the outlet oil gas of the last stage perform countercurrent heat exchange.
8. The oil gas recovery device with adjustable multi-stage condensation, adsorption and back-cabin treatment capacity of claim 1, characterized in that: fire arresters are arranged on the emptying pipeline and the cabin returning pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120531510.7U CN215916499U (en) | 2021-03-12 | 2021-03-12 | Oil gas recovery device with adjustable treatment capacity for multistage condensation, adsorption and cabin return |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120531510.7U CN215916499U (en) | 2021-03-12 | 2021-03-12 | Oil gas recovery device with adjustable treatment capacity for multistage condensation, adsorption and cabin return |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN215916499U true CN215916499U (en) | 2022-03-01 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202120531510.7U Active CN215916499U (en) | 2021-03-12 | 2021-03-12 | Oil gas recovery device with adjustable treatment capacity for multistage condensation, adsorption and cabin return |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN215916499U (en) |
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2021
- 2021-03-12 CN CN202120531510.7U patent/CN215916499U/en active Active
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