CN205275543U - Natural gas lyophilisation de -hydrocarbon system - Google Patents
Natural gas lyophilisation de -hydrocarbon system Download PDFInfo
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- CN205275543U CN205275543U CN201521130780.8U CN201521130780U CN205275543U CN 205275543 U CN205275543 U CN 205275543U CN 201521130780 U CN201521130780 U CN 201521130780U CN 205275543 U CN205275543 U CN 205275543U
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Abstract
The utility model provides a natural gas lyophilisation de -hydrocarbon system. Natural gas lyophilisation de -hydrocarbon system includes controller, precooling heat exchanger, vapour and liquid separator, heat transfer device, refrigerating plant and evacuating device, and the precooling heat exchanger is connected with vapour and liquid separator, heat transfer device includes heat exchanger I, heat exchanger II, filtering separation device I and filtering separation device II at least, and heat exchanger I and heat exchanger II's liquid outlet passes through auto -change over device and communicates with container or atmosphere respectively, refrigerating plant passes through auto -change over device and is connected with heat exchanger I and heat exchanger II respectively, and refrigerating plant is connected with the controller, evacuating device passes through auto -change over device and is connected with heat exchanger I and heat exchanger II's liquid outlet respectively, and evacuating device is connected with the controller. The utility model discloses a natural gas lyophilisation de -hydrocarbon system thoroughly defrosts to the heat exchanger through refrigerating plant and evacuating device, and it is stifled to prevent that the pipeline from freezing, need not add the inhibitor to reduced the running cost, and the device can set up lessly.
Description
Technical field
The utility model relates to the technical field of the de-hydrocarbon of Sweet natural gas lyophilization, in particular to a kind of Sweet natural gas lyophilization de-hydrocarbon system.
Background technology
Sweet natural gas out and associated gas are just exploited, general containing a large amount of aqueous vapor, when they are carried, it is transported to the position that envrionment temperature is relatively low, water can directly freeze or with natural gas adsorption hydrate, reduce the circulating capacity of collection gas pipe line on the one hand, the blocking of pipeline, valve, instrument etc. time serious, can be caused, thus affect the safety and economic operation of collection gas pipe line; Also can accelerate to collect the corrosion of gas pipe line simultaneously. In order to prevent hydrate from generating, reduce the corrosion of equipment and pipeline etc., de-hydrocarbon process of usually Sweet natural gas and associated gas being dewatered before carrying out conveying.
Hydrocarbon is taken off in order to meet the dehydration of gas transmission requirement, its dew point requires lower, as GB17820-2012 " Sweet natural gas " just defines " under interface point pressure; water dew point should minimum envrionment temperature be low 5 DEG C than under transport condition ", as can be seen here, the dew point of transport gas is required in fact not high, just " shallow de-".
The de-hydrocarbon method of conventional gas dehydration comprises molecular sieve adsorption, triglycol evaporation or adds the lyophilization method of inhibitor. These three kinds of methods respectively have relative merits, are applicable to need the occasion of low dew point as molecular sieve adsorption, and its dew point that can reach is generally-40 DEG C ~-80 DEG C, and the regeneration energy consumption of molecular sieve is relatively big, and the recycling of resurgent gases is comparatively difficult; Triglycol evaporation is applicable to the occasion of atm number, and construction cost and running cost are all relatively big, and the Sweet natural gas Gu Jing less for tolerance is not too applicable; The requirement of " shallow de-" when the lyophilization method of interpolation inhibitor is relatively applicable to natural gas transport, but the regeneration of inhibitor or consumption can increase running cost, the regeneration system rapidly of inhibitor makes device comparatively huge, and due to coefficient of heat transfer when refrigeration agent and gas (Sweet natural gas) heat exchange less, interchanger need to design bigger, therefore the refrigerant side of interchanger need to fill more refrigeration agent, it is easy to cause oil return not smooth, damage refrigerator.
Practical novel content
First object of the present utility model is to provide a kind of Sweet natural gas lyophilization de-hydrocarbon system, prior art adopt the lyophilization method adding inhibitor dewatered by Sweet natural gas de-hydrocarbon to solve, the regeneration of inhibitor or consumption can increase running cost, and the regeneration system rapidly of inhibitor makes device comparatively huge, it is not easy to the technical matters of transport.
2nd object of the present utility model is to provide a kind of oil-gas recovery device.
The utility model object is realized by following technical scheme:
A kind of Sweet natural gas lyophilization de-hydrocarbon system, comprises controller, precool heat exchanger device, gas-liquid separator, heat-exchanger rig, refrigeration plant and vacuum extractor, wherein,
Described precool heat exchanger device is connected with described gas-liquid separator;
Described heat-exchanger rig at least comprises interchanger I, interchanger II, filtering separation device I and filtering separation device II, described gas-liquid separator is connected with described interchanger I and interchanger II by shifter respectively, the air outlet of described interchanger I is connected with described filtering separation device I, the air outlet of described interchanger II is connected with described filtering separation device II, and described interchanger I is connected with pressure release device by shifter respectively with the air outlet of described interchanger II;
Described refrigeration plant is for providing cold source and thermal source to described interchanger I and described interchanger II, and described refrigeration plant is connected with described interchanger I and described interchanger II by shifter respectively, and described refrigeration plant is connected with described controller;
Described vacuum extractor is for vacuumizing described interchanger I and described interchanger II, and described vacuum extractor is connected with the air outlet of described interchanger I and described interchanger II by shifter respectively, and described vacuum extractor is connected with described controller.
Preferably, described vacuum extractor comprises vacuum pump, and described vacuum pump is connected by the air outlet of shifter with described interchanger I and interchanger II respectively, and described vacuum pump is connected with described controller.
Preferably, described refrigeration plant comprises accumulation of heat tank, hydrothermal solution pump, condenser I, throttling valve, vaporizer, compressor, cold liquid pump and stores cold tank, wherein,
Described accumulation of heat tank and the cold tank of described storage are built with secondary refrigerant;
Described accumulation of heat tank is connected by the secondary refrigerant import of described hydrothermal solution pump with described condenser I, the secondary refrigerant outlet of described condenser I is connected with heat-exchanger rig, the refrigerant outlet of described condenser I is connected by the refrigerant inlet of described throttling valve with described vaporizer, the refrigerant outlet of described vaporizer is connected by the refrigerant inlet of described compressor with described condenser I, the cold tank of described storage is connected with the secondary refrigerant import of described vaporizer by described cold liquid pump, and the secondary refrigerant outlet of described vaporizer is connected with described heat-exchanger rig;
The secondary refrigerant import of described condenser I is connected with the secondary refrigerant outlet of described condenser I, and the refrigerant inlet of described condenser I is connected with the refrigerant outlet of described condenser I; The secondary refrigerant import of described vaporizer is connected with the secondary refrigerant outlet of described vaporizer, and the refrigerant inlet of described vaporizer is connected with the refrigerant outlet of described vaporizer; Described controller is connected with described hydrothermal solution pump, described throttling valve, described compressor and described cold liquid pump respectively.
Preferably, the secondary refrigerant outlet of described condenser I is connected with described accumulation of heat tank by shifter, and the secondary refrigerant outlet of described vaporizer is connected with the cold tank of described storage by shifter.
Preferably, described refrigeration plant also comprises equilibrium valve, it is provided with liquid level alarm I in described accumulation of heat tank, it is provided with liquid level alarm II in the cold tank of described storage, described accumulation of heat tank is connected with the cold tank of described storage by described equilibrium valve, and described controller is connected with described liquid level alarm I, described liquid level alarm II and described equilibrium valve respectively.
Preferably, described refrigeration plant also comprises condenser II, and described condenser II is connected with refrigerant outlet, the described throttling valve of described condenser I respectively.
Preferably, the air outlet of described interchanger I and interchanger II is connected with described precool heat exchanger device by shifter respectively.
Preferably, also comprise pressure reduction transmitter, the pressure reduction of described pressure reduction transmitter for measuring between the inlet mouth of described interchanger I and interchanger II and air outlet, described pressure reduction transmitter respectively inlet mouth and air outlet with described interchanger I, interchanger II be connected, described pressure reduction transmitter is connected with described controller.
Preferably, described filtering separation device I and described filtering separation device II is strainer.
Preferably, described pressure release device is selected from the wherein a kind of of container, sewage lagoon or sewer line, and described container, described sewage lagoon or described sewer line are with atmosphere or are not connected.
Preferably, the pipeline that described interchanger I is connected with described pressure release device with the air outlet of interchanger II is provided with heating unit; The pipeline that described vacuum extractor is connected with the air outlet of described interchanger I and interchanger II is provided with heating unit.
A kind of oil-gas recovery device, comprises controller, precool heat exchanger device, gas-liquid separator I, heat-exchanger rig, gas-liquid separator II, absorbent charcoal adsorber, refrigeration plant and vacuum extractor, wherein,
Described precool heat exchanger device is connected with described gas-liquid separator I;
Described heat-exchanger rig at least comprises interchanger I, interchanger II, filtering separation device I and filtering separation device II, described gas-liquid separator I is connected with described interchanger I and interchanger II by shifter respectively, the air outlet of described interchanger I is connected with described filtering separation device I, the air outlet of described interchanger II is connected with described filtering separation device II, the air outlet of described interchanger I and described interchanger II is connected with pressure release device by shifter respectively, the air outlet of described interchanger I and described interchanger II is connected with described gas-liquid separator II by shifter respectively,
Described refrigeration plant is for providing cold source and thermal source to described interchanger I and described interchanger II, and described refrigeration plant is connected with described interchanger I and described interchanger II by shifter respectively, and described refrigeration plant is connected with described controller;
Described vacuum extractor is for vacuumizing described interchanger I and described interchanger II, and described vacuum extractor is connected with the air outlet of described interchanger I and described interchanger II by shifter respectively, and described vacuum extractor is connected with described controller;
Described gas-liquid separator II is connected with described absorbent charcoal adsorber.
Preferably, described refrigeration plant comprises accumulation of heat tank, hydrothermal solution pump, condenser I, throttling valve, vaporizer, compressor, cold liquid pump and stores cold tank, wherein,
Described accumulation of heat tank and the cold tank of described storage are built with secondary refrigerant;
Described accumulation of heat tank is connected by the secondary refrigerant import of described hydrothermal solution pump with described condenser I, the secondary refrigerant outlet of described condenser I is connected with heat-exchanger rig, the refrigerant outlet of described condenser I is connected by the refrigerant inlet of described throttling valve with described vaporizer, the refrigerant outlet of described vaporizer is connected by the refrigerant inlet of described compressor with described condenser I, the cold tank of described storage is connected with the secondary refrigerant import of described vaporizer by described cold liquid pump, and the secondary refrigerant outlet of described vaporizer is connected with described heat-exchanger rig;
The secondary refrigerant import of described condenser I is connected with the secondary refrigerant outlet of described condenser I, and the refrigerant inlet of described condenser I is connected with the refrigerant outlet of described condenser I; The secondary refrigerant import of described vaporizer is connected with the secondary refrigerant outlet of described vaporizer, and the refrigerant inlet of described vaporizer is connected with the refrigerant outlet of described vaporizer; Described controller is connected with described hydrothermal solution pump, described throttling valve, described compressor and described cold liquid pump respectively.
Preferably, the secondary refrigerant outlet of described condenser I is connected with described accumulation of heat tank by shifter, and the secondary refrigerant outlet of described vaporizer is connected with the cold tank of described storage by shifter.
Preferably, described refrigeration plant also comprises equilibrium valve, it is provided with liquid level alarm I in described accumulation of heat tank, it is provided with liquid level alarm II in the cold tank of described storage, described accumulation of heat tank is connected with the cold tank of described storage by described equilibrium valve, and described controller is connected with described liquid level alarm I, described liquid level alarm II and described equilibrium valve respectively; Described refrigeration plant also comprises condenser II, and described condenser II is connected with refrigerant outlet, the described throttling valve of described condenser I respectively.
Preferably, the pipeline that the air outlet of described interchanger I and interchanger II is connected with described pressure release device is provided with heating unit; The pipeline that described vacuum extractor is connected with the air outlet of described interchanger I and interchanger II is provided with heating unit.
Compared with prior art, the utility model has following useful effect:
1, Sweet natural gas lyophilization de-hydrocarbon system of the present utility model is thoroughly defrosted by refrigeration plant and vacuum extractor heat exchanging device, can prevent pipe freezeup, it is not necessary to adds inhibitor, thus reduces running cost, and device can arrange less;
2, refrigeration plant of the present utility model is equipped with the accumulation of heat tank of secondary refrigerant by setting and is stored cold tank and makes refrigerant side not need to fill too much refrigeration agent, can avoid the phenomenon occurring oil return not smooth.
Accompanying drawing explanation
Fig. 1 is the structural representation of the Sweet natural gas lyophilization de-hydrocarbon system of embodiment 1;
Fig. 2 is the structural representation of the oil-gas recovery device of embodiment 3;
Fig. 3 is the structural representation of the oil-gas recovery device that the oil-gas recovery method of embodiment 5 uses;
Fig. 4 is the structural representation of the oil-gas recovery device that the oil-gas recovery method of embodiment 6 uses.
Embodiment
Below in conjunction with accompanying drawing, the utility model is specifically described. In order to enable those skilled in the art to clear, complete knowing content of the present utility model and the technical solution of the utility model can be implemented, embodiment discloses a large amount of details. But, it is clear that ground, it does not have the technician of these details this areas also can implement the technical solution of the utility model, reaches the purpose of this utility model, it is achieved effect of the present utility model. These details are the enforcement modes of the optimum that contriver selects through a large amount of experiments, are not used for limiting protection domain of the present utility model. Protection domain of the present utility model is as the criterion with the content of claim book, and the technical scheme that the technician of this area content disclosed in present specification obtains without the need to creative work is also in protection domain of the present utility model.
Embodiment 1
Referring to Fig. 1, the present embodiment provides a kind of Sweet natural gas lyophilization de-hydrocarbon system, comprises controller, precool heat exchanger device 1, gas-liquid separator 2, heat-exchanger rig, refrigeration plant and vacuum extractor, wherein,
Described precool heat exchanger device 1 is connected with described gas-liquid separator 2;
Described heat-exchanger rig at least comprises interchanger I31, interchanger II33, filtering separation device I32 and filtering separation device II34, described gas-liquid separator 2 is connected with described interchanger I31 and interchanger II33 by switching valve 802,803 respectively, the air outlet of described interchanger I31 is connected with described filtering separation device I32, the air outlet of described interchanger II33 is connected with described filtering separation device II34, and described interchanger I31 is connected with pressure release device by switching valve 806,807,808 respectively with the air outlet of described interchanger II33;
Described refrigeration plant is for providing cold source and thermal source to described interchanger I31 and described interchanger II33, and described refrigeration plant is connected with described interchanger I31 and described interchanger II33 by switching valve respectively, and described refrigeration plant is connected with described controller;
Described vacuum extractor is for vacuumizing described interchanger I31 and described interchanger II33, described vacuum extractor is connected with the air outlet of described interchanger I31 and described interchanger II33 by switching valve 806,807 respectively, and described vacuum extractor is connected with described controller. Sweet natural gas lyophilization de-hydrocarbon system of the present utility model is thoroughly defrosted by refrigeration plant and vacuum extractor heat exchanging device, can prevent pipe freezeup, it is not necessary to adds inhibitor, thus reduces running cost, and device can arrange less.
Wherein, described filtering separation device I32 and described filtering separation device II34 is strainer. Described filtering separation device I32 can be arranged on the air outlet place of described interchanger I31, it is also possible to is arranged on pipeline that the air outlet with described interchanger I31 is connected. Described filtering separation device II34 can be arranged on the air outlet place of described interchanger II33, it is also possible to is arranged on pipeline that the air outlet with described interchanger II33 is connected. The solid matter that described filtering separation device I32 and described filtering separation device II34 gets off for tackling condensation. In this example, described heat-exchanger rig only includes two, i.e. interchanger I31 and interchanger II33, it is possible to be set to three or more than three as required.
Implementing mode as one, described vacuum extractor comprises vacuum pump 4, and described vacuum pump 4 is connected with the air outlet of described interchanger I31 and interchanger II33 by switching valve 806,807 respectively, and described vacuum pump 4 is connected with described controller. Described interchanger I31 and described interchanger II33 can be vacuumized by arranging described vacuum pump 4.
As one preferred embodiment, the pipeline that described vacuum pump 4 is connected with the air outlet of described interchanger I31 and interchanger II32 is provided with heating unit, and heating unit can be heating tape 6, can prevent pipe freezeup.
Implementing mode as one, described refrigeration plant comprises accumulation of heat tank 51, hydrothermal solution pump 52, condenser I53, throttling valve 55, vaporizer 56, compressor 57, cold liquid pump 58 and stores cold tank 59, wherein,
Described accumulation of heat tank 51 and the cold tank 59 of described storage are built with secondary refrigerant;
Described accumulation of heat tank 51 is connected by the secondary refrigerant import of described hydrothermal solution pump 52 with described condenser I53, the secondary refrigerant outlet of described condenser I53 is connected with described interchanger I31 and interchanger II33 by switching valve respectively, the refrigerant outlet of described condenser I53 is connected by the refrigerant inlet of described throttling valve 55 with described vaporizer 56, the refrigerant outlet of described vaporizer 56 is connected by the refrigerant inlet of described compressor 57 with described condenser I53, the cold tank of described storage 59 is connected with the secondary refrigerant import of described vaporizer 56 by described cold liquid pump 58, the secondary refrigerant outlet of described vaporizer 56 is connected with described interchanger I31 and interchanger II33 by switching valve respectively,
The secondary refrigerant import of described condenser I53 is connected with the secondary refrigerant outlet of described condenser I53, and the refrigerant inlet of described condenser I53 is connected with the refrigerant outlet of described condenser I53; The secondary refrigerant import of described vaporizer 56 is connected with the secondary refrigerant outlet of described vaporizer 56, and the refrigerant inlet of described vaporizer 56 is connected with the refrigerant outlet of described vaporizer 56; Described controller is connected with described hydrothermal solution pump 52, described throttling valve 55, described compressor 57 and described cold liquid pump 58 respectively. The accumulation of heat tank that refrigeration plant of the present utility model is equipped with secondary refrigerant by arranging and the cold tank of storage make refrigerant side not need to fill too much refrigeration agent, can avoid the phenomenon occurring oil return not smooth.
Wherein, secondary refrigerant can adopt any one secondary refrigerant of the prior art, as tolerated the alcohol class or silicone oil etc. of high/low temperature. The Cooling and Heat Source of refrigerator is made to be obtained for utilization by arranging described accumulation of heat tank 51 and the cold tank 59 of described storage, utilization ratio height. When refrigerator and liquid secondary refrigerant heat exchange, belong to tradition refrigeration, it is possible to adopting tradition plate-type heat exchanger, heat transfer coefficient height, oil return is good, refrigerator stable performance, make use of the cold of refrigerator and heat simultaneously, again can cold-storage and thermal storage, saved the energy. According to dew point requirement, it is desired to time not high, refrigerator can be shut down, it is not necessary to refrigerator 24 hours runs continuously, it is to increase the stability of refrigerator.
As one preferred embodiment, the secondary refrigerant outlet of described condenser I53 is connected with described accumulation of heat tank 51 by switching valve 817, and the secondary refrigerant outlet of described vaporizer 56 is connected by the cold tank 59 of switching valve 819 and described storage. When not needing defrosting and refrigeration, it is possible to starting internal recycle by opening switching valve 817 or switching valve 819, described accumulation of heat tank 51 and the cold tank 59 of described storage can store energy, avoid energy wastage. Internal recycle is the temperature storing secondary refrigerant in cold tank and accumulation of heat tank to maintain, and don't starts to the interchanger quantity of heat given up (or cold) of Sweet natural gas, stores cold tank and accumulation of heat tank can make secondary refrigerant store temporary transient no heat or cold. Such as, heat exchanging device to export cold, and when temporarily not needing quantity of heat given up, so that it may to start the internal recycle of hydrothermal solution system, to allow secondary refrigerant heat up, store heat, and not quantity of heat given up.
The temperature control of described accumulation of heat tank 51 between 30 ~ 100 DEG C, the temperature of the cold tank 59 of described storage according to gas dew point need arrange, general control is between-85 ~ 10 DEG C.
As one preferred embodiment, described refrigeration plant also comprises equilibrium valve 818, it is provided with liquid level alarm I in described accumulation of heat tank 51, it is provided with liquid level alarm II in the cold tank 59 of described storage, described accumulation of heat tank 51 is connected by the cold tank 59 of described equilibrium valve 818 and described storage, and described controller is connected with described liquid level alarm I, described liquid level alarm II and described equilibrium valve 818 respectively. After any one liquid level alarm in described liquid level alarm I, described liquid level alarm II is reported to the police, controller balances valve 818 and sends signal equilibrium valve 818 is opened, secondary refrigerant in described accumulation of heat tank 51, the cold tank of described storage 59 by liquid level high to flow to liquid level low, finally make the liquid level of two storage tanks consistent, to improve the security of two storage tanks.
As one preferred embodiment, described refrigeration plant also comprises condenser II54, and described condenser II54 is connected with refrigerant outlet, the described throttling valve 55 of described condenser I53 respectively. When the secondary refrigerant in accumulation of heat tank 51 can not total condensation refrigeration agent time, it is necessary to cooled by described condenser II54.
As one preferred embodiment, the air outlet of described interchanger I31 and interchanger II33 is connected with described precool heat exchanger device 1 by switching valve respectively. Carry out, through described precool heat exchanger device 1, the cold that heat exchange can make full use of the gas separated, it is to increase the utilization ratio of energy, save energy from described interchanger I31 and interchanger II33 gas out.
As one preferred embodiment, also comprise pressure reduction transmitter 7, the pressure reduction of described pressure reduction transmitter 7 for measuring between the inlet mouth of described interchanger I31 and interchanger II33 and air outlet, described pressure reduction transmitter 7 respectively inlet mouth and air outlet with described interchanger I31, interchanger II33 be connected, described pressure reduction transmitter 7 is connected with described controller. By arranging the pressure reduction that described pressure reduction transmitter 7 can be convenient to measure between the inlet mouth of described interchanger I31 and interchanger II33 and air outlet, when pressure reduction between the inlet mouth and air outlet of described interchanger I31 and interchanger II33 exceedes set(ting)value, described pressure reduction transmitter 7 controls the switching of the working order between described interchanger I31 and interchanger II33 to described controller transmission signal by described controller.
Further, described pressure release device is selected from the wherein a kind of of container, sewage lagoon or sewer line, and described container, described sewage lagoon or described sewer line are with atmosphere or are not connected. In the present embodiment, described pressure release device is sewer line, and described interchanger I31 is connected with sewer line by switching valve 806,807,808 respectively with the air outlet of described interchanger II33.
As one preferred embodiment, the pipeline that described interchanger I31 is connected with sewer line with the air outlet of interchanger II33 is provided with heating unit, and heating unit can be heating tape 6, can prevent pipe freezeup.
Embodiment 2
Referring to Fig. 1, the present embodiment provides the method for the de-hydrocarbon of a kind of Sweet natural gas lyophilization, comprises the following steps:
Step a: the Sweet natural gas through pre-treatment (separating major part free-water and granule foreign) enters precool heat exchanger device 1 and carries out heat exchange, make the temperature of Sweet natural gas be down to 0 ~ 25 DEG C (this temperature range be gas hydrate formed point on about 5 DEG C), enter gas-liquid separator 2 afterwards and carry out gas-liquid separation, the gas separated enters interchanger I31 by switching valve 802 and carries out heat exchange, gas is down to-80 ~+10 DEG C (lower than required water dew point or hydrocarbon dew point 5 ~ 20 DEG C) in interchanger I31, gas-liquid separation is carried out afterwards in interchanger I31, the gas of low temperature is sent, the gas of low temperature can directly be carried or enter after precool heat exchanger device 1 carries out heat exchange and carry, can automatically control to enter the amount of the cryogenic gas of precool heat exchanger device 1 by variable valve 801, make the Sweet natural gas of precooling can not form hydrate in precool heat exchanger device 1, the air outlet of interchanger I31 is provided with filtering separation device I32, and solid matter is filtered tripping device I32 and tackles, wherein, the heat exchanging process of described interchanger I31 comprises the following steps:
Cold liquid pump 58 starts, by described cold liquid pump 58, the coolant pump stored in cold tank 59 is entered in vaporizer 56, secondary refrigerant is formed the secondary refrigerant of low temperature in vaporizer 56 by cooling, the secondary refrigerant of low temperature enters described interchanger I31 through switching valve 811 from the secondary refrigerant import of described interchanger I31, make the cooling supersaturation of the Sweet natural gas in described interchanger I31, precipitate out water and/or hydrocarbon; Secondary refrigerant returns to the cold tank 59 of described storage from the outlet of the secondary refrigerant of described interchanger I31 through switching valve 809 again;
In order to improve the heat exchange effect of interchanger II33, it is possible to heat exchanging device II33 carries out precooling, and precooling process comprises the following steps:
Described interchanger I31 works after for some time, enters described interchanger II33 from the secondary refrigerant of described vaporizer 56 low temperature out through switching valve 816, makes described interchanger II33 precooling, and secondary refrigerant returns to the cold tank 59 of described storage through switching valve 814 again;
Step b: the handoff procedure being switched to described interchanger II33 by described interchanger I31, comprises the following steps:
When the pressure reduction arrived when described interchanger I31 frosting between the inlet mouth of certain time or described interchanger I31 and air outlet transfinites, the switching valve 804 of the switching valve 802 of the inlet mouth of described interchanger I31 and air outlet cuts out, the switching valve 805 of the switching valve 803 of the inlet mouth of described interchanger II33 and air outlet is opened, making the gas separated from gas-liquid separator 2 enter interchanger II33 by switching valve 803 and carry out heat exchange, the heat exchanging process of described interchanger II33 is identical with the heat exchanging process of described interchanger I31; Meanwhile, described interchanger I31 enters defrosting program, and the defrosting program of described interchanger I31 comprises the following steps:
Defrosting and pressure release bleeding stage: hydrothermal solution pump 52 starts, by described hydrothermal solution pump 52, the coolant pump in accumulation of heat tank 51 is entered in condenser I53, secondary refrigerant is warmed the secondary refrigerant forming high temperature in condenser I53, the secondary refrigerant of high temperature enters described interchanger I31 by switching valve 810 through the secondary refrigerant outlet of described interchanger I31, described interchanger I31 is heated up, the hydrate of its inside and/or ice melt and form liquid water and/or hydrocarbon, are connected with sewer line by switching valve 806,808 air outlet of described interchanger I31; Described interchanger I31 is inner was malleation (generally having certain pressure when Sweet natural gas enters interchanger) originally, after switching valve 806,808 is opened, described interchanger I31 inside and atmosphere, it is possible to the attachment of existence wax etc. on heat exchangers distils instantaneously, along with liquid water is discharged; Or when the liquid outlet of described interchanger I31 is by switching valve 806,808 and reservoir, liquid water is discharged; The secondary refrigerant of the high temperature having released heat in described interchanger I31 returns to described accumulation of heat tank 51 by switching valve 812 through the secondary refrigerant import of described interchanger I again;
Vacuumizing phase: the air outlet of described interchanger I31 is connected with vacuum pump 4, start vacuum pump 4, described interchanger I is vacuumized, makes the solid dielectric of the hydrate of described interchanger I inside, ice and/or other condensation evaporate completely or distil, namely complete defrosting program.
Water in Sweet natural gas is in the desiccated surface frosting gradually of low temperature, and frost can be blown, and can not cause the blocking of interchanger at once, if experienced by the defrosting stage, the water of chemical conversion can not be removed completely, then can build-up ice on the strainer of low temperature during cooling at once, rapidly blocking interchanger and strainer. And in the utility model, first pressure release draining, then vacuum hydro-extraction, ensure that interchanger is inner almost complete absence of free-water, during cooling refrigeration, strainer and interchanger can not be blocked rapidly again.
Embodiment 3
The present embodiment provides a kind of oil-gas recovery device, comprises controller, precool heat exchanger device 2, gas-liquid separator I3, heat-exchanger rig, gas-liquid separator II5, absorbent charcoal adsorber 6, refrigeration plant and vacuum extractor, wherein,
Described precool heat exchanger device 2 is connected with described gas-liquid separator I3;
Described heat-exchanger rig at least comprises interchanger I41, interchanger II43, filtering separation device I42 and filtering separation device II44, described gas-liquid separator I3 is respectively by switching valve 102, 103 are connected with described interchanger I41 and interchanger II43, the air outlet of described interchanger I41 is connected with described filtering separation device I42, the air outlet of described interchanger II43 is connected with described filtering separation device II44, the air outlet of described interchanger I41 and described interchanger II43 is connected with pressure release device by switching valve respectively, the air outlet of described interchanger I and described interchanger II is respectively by switching valve 108, 109 are connected with described gas-liquid separator II5,
Described refrigeration plant is for providing cold source and thermal source to described interchanger I41 and described interchanger II43, and described refrigeration plant is connected with described interchanger I41 and described interchanger II43 by switching valve respectively, and described refrigeration plant is connected with described controller;
Described vacuum extractor is for vacuumizing described interchanger I41 and described interchanger II43, described vacuum extractor is connected with the air outlet of described interchanger I41 and described interchanger II43 by shifter respectively, and described vacuum extractor is connected with described controller;
Described gas-liquid separator II5 is connected with described absorbent charcoal adsorber 6.
Oil-gas recovery device of the present utility model is thoroughly defrosted by refrigeration plant and vacuum extractor heat exchanging device, can prevent pipe freezeup, it is not necessary to adds inhibitor, thus reduces running cost.
Wherein, described filtering separation device I42 and described filtering separation device II44 is strainer. Described filtering separation device I42 can be arranged on the air outlet place of described interchanger I41, it is also possible to is arranged on pipeline that the air outlet with described interchanger I41 is connected. Described filtering separation device II44 can be arranged on the air outlet place of described interchanger II43, it is also possible to is arranged on pipeline that the air outlet with described interchanger II43 is connected. The solid matter that described filtering separation device I42 and described filtering separation device II44 gets off for tackling condensation. In this example, described heat-exchanger rig only includes two, i.e. interchanger I41 and interchanger II43, it is possible to be set to three or more than three as required.
Implementing mode as one, described refrigeration plant comprises accumulation of heat tank 81, hydrothermal solution pump 82, condenser I83, throttling valve 85, vaporizer 86, compressor 87, cold liquid pump 88 and stores cold tank 89, wherein,
Described accumulation of heat tank 81 and the cold tank 89 of described storage are built with secondary refrigerant;
Described accumulation of heat tank 81 is connected by the secondary refrigerant import of described hydrothermal solution pump 82 with described condenser I83, the secondary refrigerant outlet of described condenser I83 is connected with described interchanger I41 and described interchanger II43 by switching valve respectively, the refrigerant outlet of described condenser I83 is connected by the refrigerant inlet of described throttling valve 85 with described vaporizer 86, the refrigerant outlet of described vaporizer 86 is connected by the refrigerant inlet of described compressor 87 with described condenser I83, the cold tank of described storage 89 is connected with the secondary refrigerant import of described vaporizer 86 by described cold liquid pump 88, the secondary refrigerant outlet of described vaporizer 86 is connected with described interchanger I41 and described interchanger II43 by switching valve respectively,
The secondary refrigerant import of described condenser I83 is connected with the secondary refrigerant outlet of described condenser I83, and the refrigerant inlet of described condenser I83 is connected with the refrigerant outlet of described condenser I83; The secondary refrigerant import of described vaporizer 86 is connected with the secondary refrigerant outlet of described vaporizer 86, and the refrigerant inlet of described vaporizer 86 is connected with the refrigerant outlet of described vaporizer 86; Described controller is connected with described hydrothermal solution pump 82, described throttling valve 85, described compressor 87 and described cold liquid pump 88 respectively.
Wherein, secondary refrigerant can adopt any one secondary refrigerant of the prior art, as tolerated the alcohol class or silicone oil etc. of high/low temperature. The Cooling and Heat Source of refrigerator is made to be obtained for utilization by arranging described accumulation of heat tank 81 and the cold tank 89 of described storage, utilization ratio height. When refrigerator and liquid secondary refrigerant heat exchange, belong to tradition refrigeration, it is possible to adopting tradition plate-type heat exchanger, heat transfer coefficient height, oil return is good, refrigerator stable performance, make use of the cold of refrigerator and heat simultaneously, again can cold-storage and thermal storage, saved the energy. According to dew point requirement, it is desired to time not high, refrigerator can be shut down, it is not necessary to refrigerator 24 hours runs continuously, it is to increase the stability of refrigerator.
As one preferred embodiment, the secondary refrigerant outlet of described condenser I83 is connected with described accumulation of heat tank 81 by switching valve 116, and the secondary refrigerant outlet of described vaporizer 86 is connected by the cold tank 89 of switching valve 118 and described storage. When not needing defrosting and refrigeration, it is possible to starting internal recycle by opening switching valve 116 or switching valve 118, described accumulation of heat tank 81 and the cold tank 89 of described storage can store energy, avoid energy wastage. Internal recycle is the temperature storing secondary refrigerant in cold tank and accumulation of heat tank to maintain, and don't starts to the interchanger quantity of heat given up (or cold) of Sweet natural gas, stores cold tank and accumulation of heat tank can make secondary refrigerant store temporary transient no heat or cold. Such as, heat exchanging device to export cold, and when temporarily not needing quantity of heat given up, so that it may to start the internal recycle of hydrothermal solution system, to allow secondary refrigerant heat up, store heat, and not quantity of heat given up.
As one preferred embodiment, described refrigeration plant also comprises equilibrium valve 117, it is provided with liquid level alarm I in described accumulation of heat tank 81, it is provided with liquid level alarm II in the cold tank 89 of described storage, described accumulation of heat tank 81 is connected by the cold tank 89 of described equilibrium valve 117 and described storage, and described controller is connected with described liquid level alarm I, described liquid level alarm II and described equilibrium valve 117 respectively. After any one liquid level alarm in described liquid level alarm I, described liquid level alarm II is reported to the police, controller balances valve 117 and sends signal equilibrium valve 117 is opened, secondary refrigerant in described accumulation of heat tank 81, the cold tank of described storage 89 by liquid level high to flow to liquid level low, finally make the liquid level of two storage tanks consistent, to improve the security of two storage tanks.
As one preferred embodiment, described refrigeration plant also comprises condenser II84, and described condenser II84 is connected with refrigerant outlet, the described throttling valve 85 of described condenser I83 respectively. When the secondary refrigerant in accumulation of heat tank 81 can not total condensation refrigeration agent time, it is necessary to cooled by described condenser II84.
Implementing mode as one, described vacuum extractor comprises vacuum pump 7, and described vacuum pump 7 is connected with the air outlet of described interchanger I41 and interchanger II43 by switching valve 104,105 respectively, and described vacuum pump 7 is connected with described controller. Described interchanger I41 and described interchanger II43 can be vacuumized by arranging described vacuum pump 7.
As one preferred embodiment, described gas-liquid separator II5 is connected with described precool heat exchanger device by switching valve. Carry out, through described precool heat exchanger device 2, the cold that heat exchange can make full use of the gas separated, it is to increase the utilization ratio of energy, save energy from described gas-liquid separator II5 gas out.
As one preferred embodiment, also comprise pressure reduction transmitter 9, the pressure reduction of described pressure reduction transmitter 9 for measuring between the inlet mouth of described interchanger I41 and interchanger II43 and air outlet, described pressure reduction transmitter 9 respectively inlet mouth and air outlet with described interchanger I41, interchanger II43 be connected, described pressure reduction transmitter 9 is connected with described controller. By arranging the pressure reduction that described pressure reduction transmitter 9 can be convenient to measure between the inlet mouth of described interchanger I41 and interchanger II43 and air outlet, when pressure reduction between the inlet mouth and air outlet of described interchanger I41 and interchanger II43 exceedes set(ting)value, described pressure reduction transmitter 9 controls the switching of the working order between described interchanger I41 and interchanger II43 to described controller transmission signal by described controller.
As one preferred embodiment, the pipeline that described interchanger I41 is connected with described pressure release device with the air outlet of interchanger II43 is provided with heating unit, and heating unit can be heating tape, can prevent pipe freezeup. In the present embodiment, described pressure release device is described gas-liquid separator I3, it is possible to be other container, sewage lagoon or sewer line.
As one preferred embodiment, the pipeline that described vacuum pump 7 is connected with the air outlet of described interchanger I41 and interchanger II43 is provided with heating unit, and heating unit can be heating tape, can prevent pipe freezeup.
Embodiment 4
Referring to Fig. 2, the present embodiment provides a kind of oil-gas recovery method, comprises the following steps:
Step a: oil gas is introduced precool heat exchanger device 2 through induced draft fan 1 and carries out heat exchange, the temperature of oil gas is made to be down to 3 ~ 7 DEG C, enter gas-liquid separator I3 afterwards and carry out gas-liquid separation, the gas separated enters described interchanger I41 by switching valve 102 through the inlet mouth of interchanger I41 and carries out heat exchange, gas is down to-80 ~-10 DEG C in interchanger I41, after enter gas-liquid separator II5 through the air outlet of described interchanger I41 and carry out gas-liquid separation, the gas separated directly enters absorbent charcoal adsorber 6 through variable valve 101 and carries out de-hydrocarbon process, directly discharges afterwards; Or the gas separated is introduced into precool heat exchanger device 2 and carries out heat exchange, enter absorbent charcoal adsorber 6 afterwards again and carry out de-hydrocarbon process; The air outlet of interchanger I41 is provided with filtering separation device I42, and solid matter is filtered tripping device I42 and tackles; Wherein, the heat exchanging process of described interchanger I41 comprises the following steps:
Cold liquid pump 88 starts, by described cold liquid pump 88, the coolant pump stored in cold tank 89 is entered in vaporizer 86, secondary refrigerant is formed the secondary refrigerant of low temperature in vaporizer 86 by cooling, the secondary refrigerant of low temperature enters described interchanger I41 through switching valve 113 from the secondary refrigerant import of described interchanger I41, make the cooling supersaturation of the oil gas in described interchanger I41, precipitate out water and/or hydrocarbon; Secondary refrigerant returns to the cold tank 89 of described storage from the outlet of the secondary refrigerant of described interchanger I41 through switching valve 111 again;
In order to improve the heat exchange effect of interchanger II43, it is possible to heat exchanging device II43 carries out precooling, and precooling process comprises the following steps:
Described interchanger I41 works after for some time, enters described interchanger II43 from the secondary refrigerant of described vaporizer 86 low temperature out through switching valve 115, makes described interchanger II43 precooling, and secondary refrigerant returns to the cold tank 89 of described storage through switching valve 114 again;
Step b: the handoff procedure being switched to described interchanger II by described interchanger I, comprises the following steps:
The switching valve 108 of the switching valve 102 of the inlet mouth of described interchanger I41 and air outlet cuts out, the switching valve 109 of the switching valve 103 of the inlet mouth of described interchanger II43 and air outlet is opened, making the gas separated from gas-liquid separator I3 enter described interchanger II43 by switching valve 103 through the inlet mouth of described interchanger II43 and carry out heat exchange, the heat exchanging process of described interchanger II43 is identical with the heat exchanging process of described interchanger I41; Meanwhile, described interchanger I41 enters defrosting program, and the defrosting program of described interchanger I41 comprises the following steps:
Defrosting and bleeding stage: hydrothermal solution pump 82 starts, by described hydrothermal solution pump 82, the coolant pump in accumulation of heat tank 81 is entered in condenser I83, secondary refrigerant is warmed the secondary refrigerant forming high temperature in condenser I83, the secondary refrigerant of high temperature enters described interchanger I41 by switching valve 110 through the secondary refrigerant outlet of described interchanger I41, described interchanger I41 is heated up, the hydrate of its inside and/or ice melt and form liquid water and/or hydrocarbon, and from the air outlet discharge of described interchanger I, liquid water and/or hydrocarbon are entered after switching valve 106 gas-liquid separator I3; The secondary refrigerant of the high temperature having released heat in described interchanger I41 returns to described accumulation of heat tank 81 by switching valve 112 through the secondary refrigerant import of described interchanger I41 again;
Vacuumizing phase: the air outlet of described interchanger I is connected with vacuum pump 7 through switching valve 104, start vacuum pump 7, described interchanger I41 is vacuumized, make the solid dielectric of the hydrate of described interchanger I41 inside, ice and/or other condensation evaporate completely or distil, namely complete defrosting program.
Water in oil gas is in the desiccated surface frosting gradually of low temperature, and frost can be blown, and can not cause the blocking of interchanger at once, if experienced by the defrosting stage, the water of chemical conversion can not be removed completely, then can build-up ice on the strainer of low temperature during cooling at once, rapidly blocking interchanger and strainer. And in the utility model, first pressure release draining, then vacuum hydro-extraction, ensure that interchanger is inner almost complete absence of free-water, during cooling refrigeration, strainer and interchanger can not be blocked rapidly again, it is not necessary to add inhibitor, thus reduce running cost.
Embodiment 5
Referring to Fig. 3, the present embodiment provides a kind of oil-gas recovery method, comprises the following steps:
Step a: oil gas induced draft fan 1 is introduced absorbent charcoal adsorber I31 through switching valve I101 and carries out de-hydrocarbon process, after absorbent charcoal adsorber I31 de-hydrocarbon for some time, close described switching valve I101, oil gas is introduced absorbent charcoal adsorber II32 through switching valve II103 simultaneously and carry out de-hydrocarbon process; Hydrocarbons in absorbent charcoal adsorber I31 is aspirated through switching valve 102 with vacuum pump 6 afterwards, the hydrocarbons pumped out enters described interchanger I41 by switching valve 104 through the inlet mouth of interchanger I41 and carries out heat exchange, gas is down to-80 ~ 20 DEG C in interchanger I, after switching valve 105 through the air outlet of described interchanger I41 enter gas-liquid separator 22 and carry out gas-liquid separation, the gas separated enters absorbent charcoal adsorber II32 and carries out de-hydrocarbon process; The air outlet of interchanger I41 is provided with filtering separation device I42, and solid matter is filtered tripping device I42 and tackles; Wherein, the heat exchanging process of described interchanger I41 comprises the following steps:
Cold liquid pump 78 starts, by described cold liquid pump 78, the coolant pump stored in cold tank 79 is entered in vaporizer 76, secondary refrigerant is formed the secondary refrigerant of low temperature in vaporizer 76 by cooling, the secondary refrigerant of low temperature enters described interchanger I41 through switching valve 114 from the secondary refrigerant import of described interchanger I41, make the cooling supersaturation of the oil gas in described interchanger I41, precipitate out water and/or hydrocarbon; Secondary refrigerant returns to the cold tank 79 of described storage from the outlet of the secondary refrigerant of described interchanger I41 through switching valve 112 again;
In order to improve the heat exchange effect of interchanger II43, it is possible to heat exchanging device II43 carries out precooling, and precooling process comprises the following steps:
Described interchanger I41 works after for some time, enters described interchanger II43 from the secondary refrigerant of described vaporizer 76 low temperature out through switching valve 116, makes described interchanger II43 precooling, and secondary refrigerant returns to the cold tank 79 of described storage through switching valve 115 again;
Step b: the handoff procedure being switched to described interchanger II43 by described interchanger I41, comprises the following steps:
The switching valve 105 of the switching valve 104 of the inlet mouth of described interchanger I41 and air outlet cuts out, the switching valve 120 of the switching valve 108 of the inlet mouth of described interchanger II43 and air outlet is opened, the hydrocarbons that vacuum pump 6 is pumped out enters described interchanger II43 by switching valve 108 and carries out heat exchange, and the heat exchanging process of described interchanger II43 is identical with the heat exchanging process of described interchanger I41; Meanwhile, described interchanger I41 enters defrosting program, and the defrosting program of described interchanger I41 comprises the following steps:
Defrosting and bleeding stage: hydrothermal solution pump 72 starts, by described hydrothermal solution pump 72, the coolant pump in accumulation of heat tank 71 is entered in condenser I73, secondary refrigerant is warmed the secondary refrigerant forming high temperature in condenser I73, the secondary refrigerant of high temperature enters described interchanger I41 by switching valve 111 through the secondary refrigerant outlet of described interchanger I41, described interchanger I41 is heated up, the hydrate of its inside and/or ice melt and form liquid water and/or hydrocarbon, and from the switching valve 107 of the air outlet of described interchanger I41, liquid water and/or hydrocarbon are expelled to temporary container 21; The secondary refrigerant of the high temperature having released heat in described interchanger I41 returns to described accumulation of heat tank 71 by switching valve 113 through the secondary refrigerant import of described interchanger I41 again;
Vacuumizing phase: the air outlet of described interchanger I41 is connected with described vacuum pump 6 through switching valve 106, start described vacuum pump 6, described interchanger I41 is vacuumized, make the solid dielectric of the hydrate of described interchanger I41 inside, ice and/or other condensation evaporate completely or distil, namely complete defrosting program.
Embodiment 6
Referring to Fig. 4, the present embodiment provides a kind of oil-gas recovery method, comprises the following steps:
Step a: oil gas is introduced precool heat exchanger device 2 through induced draft fan 1 and carries out heat exchange, enter gas-liquid separator I31 afterwards and carry out gas-liquid separation, the gas separated enters absorbent charcoal adsorber I51 through switching valve I101 and carries out de-hydrocarbon process, after absorbent charcoal adsorber I51 de-hydrocarbon for some time, close switching valve I101, oil gas is introduced absorbent charcoal adsorber II52 through switching valve II103 simultaneously and carry out de-hydrocarbon process; With vacuum pump 7, the hydrocarbons in absorbent charcoal adsorber I51 is aspirated afterwards, the hydrocarbons pumped out enters described interchanger I41 by switching valve 104 through the inlet mouth of interchanger I41 and carries out heat exchange, gas is down to-80 ~ 20 DEG C in interchanger I41, after enter gas-liquid separator II32 through the air outlet of described interchanger I41 and carry out gas-liquid separation, the gas separated enters absorbent charcoal adsorber II52 and carries out de-hydrocarbon process; The air outlet of interchanger I41 is provided with filtering separation device I42, and solid matter is filtered tripping device I42 and tackles; Wherein, the heat exchanging process of described interchanger I41 comprises the following steps:
Cold liquid pump 88 starts, by described cold liquid pump 88, the coolant pump stored in cold tank 89 is entered in vaporizer 86, secondary refrigerant is formed the secondary refrigerant of low temperature in vaporizer 86 by cooling, the secondary refrigerant of low temperature enters described interchanger I41 through switching valve 114 from the secondary refrigerant import of described interchanger I41, make the cooling supersaturation of the oil gas in described interchanger I41, precipitate out water and/or hydrocarbon; Secondary refrigerant returns to the cold tank 89 of described storage from the outlet of the secondary refrigerant of described interchanger I41 through switching valve 112 again;
In order to improve the heat exchange effect of interchanger II43, it is possible to heat exchanging device II43 carries out precooling, and precooling process comprises the following steps:
Described interchanger I41 works after for some time, enters described interchanger II43 from the secondary refrigerant of described vaporizer 86 low temperature out through switching valve 116, makes described interchanger II43 precooling, and secondary refrigerant returns to the cold tank 89 of described storage through switching valve 115 again;
Step b: the handoff procedure being switched to described interchanger II43 by described interchanger I41, comprises the following steps:
The switching valve 105 of the switching valve 104 of the inlet mouth of described interchanger I41 and air outlet cuts out, the switching valve 109 of the switching valve 108 of the inlet mouth of described interchanger II43 and air outlet is opened, making hydrocarbons that vacuum pump 7 pumps out enter described interchanger II43 by switching valve 108 through the inlet mouth of described interchanger II43 and carry out heat exchange, the heat exchanging process of described interchanger II43 is identical with the heat exchanging process of described interchanger I41; Meanwhile, described interchanger I41 enters defrosting program, and the defrosting program of described interchanger I41 comprises the following steps:
Defrosting and bleeding stage: hydrothermal solution pump 82 starts, by described hydrothermal solution pump 82, the coolant pump in accumulation of heat tank 81 is entered in condenser I83, secondary refrigerant is warmed the secondary refrigerant forming high temperature in condenser I83, the secondary refrigerant of high temperature enters described interchanger I41 by switching valve 111 through the secondary refrigerant outlet of described interchanger I41, described interchanger I41 is heated up, the hydrate of its inside and/or ice melt and form liquid water and/or hydrocarbon, and from the switching valve 106 of the air outlet of described interchanger I, liquid water and/or hydrocarbon are expelled to gas-liquid separator I31; The secondary refrigerant of the high temperature having released heat in described interchanger I41 returns to described accumulation of heat tank 81 by switching valve 113 through the secondary refrigerant import of described interchanger I41 again;
Vacuumizing phase: the air outlet of described interchanger I41 is connected with described vacuum pump 7 through switching valve 107, start described vacuum pump 7, described interchanger I41 is vacuumized, make the solid dielectric of the hydrate of described interchanger I41 inside, ice and/or other condensation evaporate completely or distil, namely complete defrosting program.
Several specific embodiments being only the application disclosed in above, but the application is not limited thereto, the changes that any person skilled in the art can think of, all should drop in the protection domain of the application.
Claims (16)
1. a Sweet natural gas lyophilization de-hydrocarbon system, it is characterised in that, comprise controller, precool heat exchanger device, gas-liquid separator, heat-exchanger rig, refrigeration plant and vacuum extractor, wherein,
Described precool heat exchanger device is connected with described gas-liquid separator;
Described heat-exchanger rig at least comprises interchanger I, interchanger II, filtering separation device I and filtering separation device II, described gas-liquid separator is connected with described interchanger I and interchanger II by shifter respectively, the air outlet of described interchanger I is connected with described filtering separation device I, the air outlet of described interchanger II is connected with described filtering separation device II, and described interchanger I is connected with pressure release device by shifter respectively with the air outlet of described interchanger II;
Described refrigeration plant is for providing cold source and thermal source to described interchanger I and described interchanger II, and described refrigeration plant is connected with described interchanger I and described interchanger II by shifter respectively, and described refrigeration plant is connected with described controller;
Described vacuum extractor is for vacuumizing described interchanger I and described interchanger II, and described vacuum extractor is connected with the air outlet of described interchanger I and described interchanger II by shifter respectively, and described vacuum extractor is connected with described controller.
2. Sweet natural gas lyophilization de-hydrocarbon system as claimed in claim 1, it is characterized in that, described vacuum extractor comprises vacuum pump, and described vacuum pump is connected by the air outlet of shifter with described interchanger I and interchanger II respectively, and described vacuum pump is connected with described controller.
3. Sweet natural gas lyophilization de-hydrocarbon system as claimed in claim 1, it is characterised in that, described refrigeration plant comprises accumulation of heat tank, hydrothermal solution pump, condenser I, throttling valve, vaporizer, compressor, cold liquid pump and stores cold tank, wherein,
Described accumulation of heat tank and the cold tank of described storage are built with secondary refrigerant;
Described accumulation of heat tank is connected by the secondary refrigerant import of described hydrothermal solution pump with described condenser I, the secondary refrigerant outlet of described condenser I is connected with heat-exchanger rig, the refrigerant outlet of described condenser I is connected by the refrigerant inlet of described throttling valve with described vaporizer, the refrigerant outlet of described vaporizer is connected by the refrigerant inlet of described compressor with described condenser I, the cold tank of described storage is connected with the secondary refrigerant import of described vaporizer by described cold liquid pump, and the secondary refrigerant outlet of described vaporizer is connected with described heat-exchanger rig;
The secondary refrigerant import of described condenser I is connected with the secondary refrigerant outlet of described condenser I, and the refrigerant inlet of described condenser I is connected with the refrigerant outlet of described condenser I; The secondary refrigerant import of described vaporizer is connected with the secondary refrigerant outlet of described vaporizer, and the refrigerant inlet of described vaporizer is connected with the refrigerant outlet of described vaporizer; Described controller is connected with described hydrothermal solution pump, described throttling valve, described compressor and described cold liquid pump respectively.
4. Sweet natural gas lyophilization de-hydrocarbon system as claimed in claim 3, it is characterised in that, the secondary refrigerant outlet of described condenser I is connected with described accumulation of heat tank by shifter, and the secondary refrigerant outlet of described vaporizer is connected with the cold tank of described storage by shifter.
5. Sweet natural gas lyophilization de-hydrocarbon system as claimed in claim 3, it is characterized in that, described refrigeration plant also comprises equilibrium valve, it is provided with liquid level alarm I in described accumulation of heat tank, it is provided with liquid level alarm II in the cold tank of described storage, described accumulation of heat tank is connected with the cold tank of described storage by described equilibrium valve, and described controller is connected with described liquid level alarm I, described liquid level alarm II and described equilibrium valve respectively.
6. Sweet natural gas lyophilization de-hydrocarbon system as claimed in claim 3, it is characterised in that, described refrigeration plant also comprises condenser II, and described condenser II is connected with refrigerant outlet, the described throttling valve of described condenser I respectively.
7. Sweet natural gas lyophilization de-hydrocarbon system as claimed in claim 1, it is characterised in that, the air outlet of described interchanger I and interchanger II is connected with described precool heat exchanger device by shifter respectively.
8. Sweet natural gas lyophilization de-hydrocarbon system as claimed in claim 1, it is characterized in that, also comprise pressure reduction transmitter, the pressure reduction of described pressure reduction transmitter for measuring between the inlet mouth of described interchanger I and interchanger II and air outlet, described pressure reduction transmitter respectively inlet mouth and air outlet with described interchanger I, interchanger II be connected, described pressure reduction transmitter is connected with described controller.
9. Sweet natural gas lyophilization de-hydrocarbon system as claimed in claim 1, it is characterised in that, described filtering separation device I and described filtering separation device II is strainer.
10. Sweet natural gas lyophilization de-hydrocarbon system as claimed in claim 1, it is characterised in that, described pressure release device is selected from the wherein a kind of of container, sewage lagoon or sewer line, and described container, described sewage lagoon or described sewer line are with atmosphere or are not connected.
11. Sweet natural gas lyophilization de-hydrocarbon systems as claimed in claim 1, it is characterised in that, the pipeline that described interchanger I is connected with described pressure release device with the air outlet of interchanger II is provided with heating unit; The pipeline that described vacuum extractor is connected with the air outlet of described interchanger I and interchanger II is provided with heating unit.
12. 1 kinds of oil-gas recovery devices, it is characterised in that, comprise controller, precool heat exchanger device, gas-liquid separator I, heat-exchanger rig, gas-liquid separator II, absorbent charcoal adsorber, refrigeration plant and vacuum extractor, wherein,
Described precool heat exchanger device is connected with described gas-liquid separator I;
Described heat-exchanger rig at least comprises interchanger I, interchanger II, filtering separation device I and filtering separation device II, described gas-liquid separator I is connected with described interchanger I and interchanger II by shifter respectively, the air outlet of described interchanger I is connected with described filtering separation device I, the air outlet of described interchanger II is connected with described filtering separation device II, the air outlet of described interchanger I and described interchanger II is connected with pressure release device by shifter respectively, the air outlet of described interchanger I and described interchanger II is connected with described gas-liquid separator II by shifter respectively,
Described refrigeration plant is for providing cold source and thermal source to described interchanger I and described interchanger II, and described refrigeration plant is connected with described interchanger I and described interchanger II by shifter respectively, and described refrigeration plant is connected with described controller;
Described vacuum extractor is for vacuumizing described interchanger I and described interchanger II, and described vacuum extractor is connected with the air outlet of described interchanger I and described interchanger II by shifter respectively, and described vacuum extractor is connected with described controller;
Described gas-liquid separator II is connected with described absorbent charcoal adsorber.
13. oil-gas recovery devices as claimed in claim 12, it is characterised in that, described refrigeration plant comprises accumulation of heat tank, hydrothermal solution pump, condenser I, throttling valve, vaporizer, compressor, cold liquid pump and stores cold tank, wherein,
Described accumulation of heat tank and the cold tank of described storage are built with secondary refrigerant;
Described accumulation of heat tank is connected by the secondary refrigerant import of described hydrothermal solution pump with described condenser I, the secondary refrigerant outlet of described condenser I is connected with heat-exchanger rig, the refrigerant outlet of described condenser I is connected by the refrigerant inlet of described throttling valve with described vaporizer, the refrigerant outlet of described vaporizer is connected by the refrigerant inlet of described compressor with described condenser I, the cold tank of described storage is connected with the secondary refrigerant import of described vaporizer by described cold liquid pump, and the secondary refrigerant outlet of described vaporizer is connected with described heat-exchanger rig;
The secondary refrigerant import of described condenser I is connected with the secondary refrigerant outlet of described condenser I, and the refrigerant inlet of described condenser I is connected with the refrigerant outlet of described condenser I; The secondary refrigerant import of described vaporizer is connected with the secondary refrigerant outlet of described vaporizer, and the refrigerant inlet of described vaporizer is connected with the refrigerant outlet of described vaporizer; Described controller is connected with described hydrothermal solution pump, described throttling valve, described compressor and described cold liquid pump respectively.
14. oil-gas recovery devices as claimed in claim 13, it is characterised in that, the secondary refrigerant outlet of described condenser I is connected with described accumulation of heat tank by shifter, and the secondary refrigerant outlet of described vaporizer is connected with the cold tank of described storage by shifter.
15. oil-gas recovery devices as claimed in claim 13, it is characterized in that, described refrigeration plant also comprises equilibrium valve, it is provided with liquid level alarm I in described accumulation of heat tank, it is provided with liquid level alarm II in the cold tank of described storage, described accumulation of heat tank is connected with the cold tank of described storage by described equilibrium valve, and described controller is connected with described liquid level alarm I, described liquid level alarm II and described equilibrium valve respectively; Described refrigeration plant also comprises condenser II, and described condenser II is connected with refrigerant outlet, the described throttling valve of described condenser I respectively.
16. oil-gas recovery devices as claimed in claim 12, it is characterised in that, the pipeline that the air outlet of described interchanger I and interchanger II is connected with described pressure release device is provided with heating unit; The pipeline that described vacuum extractor is connected with the air outlet of described interchanger I and interchanger II is provided with heating unit.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106367147A (en) * | 2016-09-27 | 2017-02-01 | 陈朝晖 | Natural gas dehydration system and dehydration method thereof |
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