CN205011721U - Smart dewatering system of synthesis of LNGLPGNGL product is retrieved to saturation wet oil associated gas - Google Patents
Smart dewatering system of synthesis of LNGLPGNGL product is retrieved to saturation wet oil associated gas Download PDFInfo
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- CN205011721U CN205011721U CN201520659080.1U CN201520659080U CN205011721U CN 205011721 U CN205011721 U CN 205011721U CN 201520659080 U CN201520659080 U CN 201520659080U CN 205011721 U CN205011721 U CN 205011721U
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Abstract
The utility model belongs to the technical field of the oil gas field exploitation, relate to the associated gas and retrieve, concretely relates to smart dewatering system of synthesis of LNGLPGNGL product is retrieved to saturation wet oil associated gas, including the pressure boost of raw materials associated gas and purification unit, LPG cold box unit, heavy hydrocarbon fractionation unit and LNG cold box unit, to the characteristics of medium component, adopted different kinds of molecular sieves to make up, to the dehydration requirement of difference, adopted high -low pressure tandem compound dehydration mode, satisfy the requirement of different water dew points respectively, adopted high -pressure purification stingy as the regeneration gas, the influence of regeneration gas to regeneration effect has been avoided in the dehydration regeneration of establishing ties to the high -low pressure. Hierarchical dehydration, the thinking is novel, advanced technology, the energy consumption is lower, and the operation is stable, and it is convenient to maintain.
Description
Technical field
The utility model belongs to exploitation of oil-gas field technical field, is specifically related to the comprehensive smart dewatering system that a kind of saturated aqueous oil field gas reclaims LNG/LPG/NGL product.
Background technology
Associated gas (being often referred to the Sweet natural gas with oil symbiosis) is oil field oil field gas, it is the volatile part of crude oil, belonging to malthenes inflammable gas, is high-grade fuel and industrial chemicals, is mainly derived from oil well casing, website gas-liquid separation, oil tank volatilization and stabilization of crude oil etc.
In the past, disperseed due to associated gas and measured little, complex treatment process, invest higher, mostly take the mode process such as burning or direct discharge, this both polluted environment, waste resource, there is potential safety hazard simultaneously, energy-conservation with the whole world, reduce discharging, low-carbon economy do not conform to the theory of Green Development.
Associated gas has very high economic worth.Associated gas after treatment, callable economic product has: LPG(liquefied petroleum gas (LPG)), NGL(stable light hydrocarbon or mixed hydrocarbon) and dry gas (Sweet natural gases of de-lighter hydrocarbons), dry gas is except the fuel gas as point on duty, process furnace, thermal oil and generator, remaining dry gas can produce CNG(compressed natural gas) and LNG(natural gas liquids), when tolerance is larger, also can be used for building gas transmission line export trade.
In associated gas recovery technology, define the conventional typical process being separated into representative with condensation fractionation, DXH technique, cold oil absorption, self-produced lime set refrigeration and supersonic speed at present, but these techniques all only produce LPG, NGL and dry gas, the object of its dehydration is the requirement of the safe operation meeting ice chest, generally low than associated gas minimum operating temperature 5 DEG C ~ 10 DEG C.
Associated gas conventional recycling processes is not high due to dehydration depth requirements, adopts low pressure 1 grade of dehydration to meet the demands; Conventional gas produces LNG, because its pressure is high, not containing heavy hydrocarbon, adopts 1 grade of dehydration to meet the demands.
Reclaim LNG product for associated gas, low-pressure first-stage dehydration cannot meet high precision dehydration requirement, as adopted high pressure 1 grade dehydration, though dehydration precision can meet and will go, but heavy hydrocarbon water content exceeds standard, there is the risk of frozen block in heavy hydrocarbon fractionating system, and liquefied gas index does not meet product index requirement.
Utility model content
The purpose of this utility model is the comprehensive smart dewatering process system of one developed for saturated aqueous associated gas remanufacture LNG, LPG and NGL product, solve the LNG product adopting associated gas conventional recycling processes to reclaim, there is heavy hydrocarbon water content to exceed standard, there is the risk of frozen block in heavy hydrocarbon fractionating system, liquefied gas index does not meet the problem of product index requirement.
For this reason, the utility model provides the comprehensive smart dewatering system that a kind of saturated aqueous oil field gas reclaims LNG/LPG/NGL product, comprises raw material associated gas pressurizing and clean unit, LPG cold box unit, heavy hydrocarbon fractionation unit and LPG cold box unit.
Described raw material associated gas pressurizing and clean unit are prized by the first gas-liquid separator connected successively, stage compressor, the second gas-liquid separator, desulfurization and decarburization device and dehydration technology and are formed.
Described LPG cold box unit is made up of solid method fine de-sulfur equipment, two stage compressor, the 3rd gas-liquid separator, LPG ice chest, Gu method fine de-sulfur equipment connection dehydration technology sled), Gu method fine de-sulfur equipment, two stage compressor, the 3rd gas-liquid separator connect successively, the outlet line of the 3rd gas-liquid separator is through LPG ice chest.
Described heavy hydrocarbon fractionation unit comprises heavy hydrocarbon washing tower, heavy hydrocarbon deethanizing column, mixed hydrocarbon debutanizing tower and high press-dehydrating sled, the outlet line of described 3rd gas-liquid separator is communicated with heavy hydrocarbon washing tower after LPG ice chest, the tower bottom outlet pipeline of heavy hydrocarbon washing tower is communicated with heavy hydrocarbon deethanizing column, the tower top outlet pipeline of heavy hydrocarbon deethanizing column exports as methane rich overhead gas after LPG ice chest, the tower bottom outlet pipeline of heavy hydrocarbon deethanizing column connects mixed hydrocarbon debutanizing tower, the tower top outlet of mixed hydrocarbon debutanizing tower is LPG outlet, and the tower bottom outlet of mixed hydrocarbon debutanizing tower is NGL outlet; The tower top outlet pipeline of heavy hydrocarbon washing tower is communicated with high press-dehydrating sled after LPG ice chest.
Described LPG cold box unit comprises LNG ice chest and denitrogenation stripping tower, the outlet line of described high press-dehydrating sled is by being communicated to denitrogenation stripping tower after LNG ice chest, the tower top outlet of denitrogenation stripping tower is rich nitrogen offgas outlet, and the tower bottom outlet pipeline of denitrogenation stripping tower is again by being communicated to LNG storage tank after LNG ice chest.
Being provided with resurgent gases in described high press-dehydrating sled goes dehydration technology to export, and is provided with resurgent gases from high press-dehydrating entrance in described dehydration technology sled, and resurgent gases connects resurgent gases from high press-dehydrating entrance and goes dehydration technology to export.
Described dehydration technology sled comprises low pressure molecular dehydration adsorption tower A, low pressure molecular dehydration regenerator column, water cooler one and electric heater one.
The tower top fairlead of described low pressure molecular dehydration adsorption tower A and low pressure molecular dehydration regenerator column B is divided into two-way, leads up to valve A1, B1 to be connected with low pressure associated gas inlet pipe, separately leads up to valve A2, B2 to be connected with the inlet pipe of water cooler one; Described low pressure associated gas inlet pipe is provided with a unstripped gas strainer one, and the escape pipe of described water cooler one is connected to water separator inlet pipe, and the escape pipe of water separator is connected to unstripped gas strainer one inlet pipe.
The tower reactor fairlead of described low pressure molecular dehydration adsorption tower A and low pressure molecular dehydration regenerator column B is also divided into two-way, leading up to valve A3, B3 is connected with dehydration associated gas escape pipe, separately leading up to valve A4, B4 is connected with the escape pipe of electric heater one, and the inlet mouth of electric heater one is communicated with the air outlet of interchanger one; Described dehydration associated gas escape pipe is provided with a dust filter unit one, the inlet mouth of described interchanger one connects resurgent gases from high press-dehydrating entrance, resurgent gases is also connected with the inlet pipe of water cooler one from high press-dehydrating entrance, and the escape pipe of described electric heater one is also connected to the inlet pipe of water cooler one.
Molecular sieve in described low pressure molecular dehydration adsorption tower A, low pressure molecular dehydration regenerator column B is 3A type molecular sieve.
Described high press-dehydrating sled comprises high pressure molecular dehydration adsorption tower, high pressure molecular dehydration regenerator column D, water cooler two and electric heater two.
The tower top fairlead of described high pressure molecular dehydration adsorption tower C and high pressure molecular dehydration regenerator column D is divided into two-way, leads up to valve C1, D1 to be connected with high pressure associated gas inlet pipe, separately leads up to valve C2, D2 to be connected with the inlet pipe of water cooler two; Described high pressure associated gas inlet pipe is provided with a unstripped gas strainer two, and the escape pipe of described water cooler is connected to resurgent gases and goes dehydration technology to export.
The tower reactor fairlead of described high pressure molecular dehydration adsorption tower C and low pressure molecular dehydration regenerator column D is also divided into two-way, leading up to valve C3, D3 is connected with dehydration associated gas escape pipe, separately leading up to valve C4, D4 is connected with the escape pipe of electric heater two, and the inlet mouth of electric heater two is communicated with the air outlet of interchanger two; Described dehydration associated gas escape pipe is provided with a dust filter unit two and a demercuration tower, the inlet mouth of described interchanger two is connected to dehydration associated gas escape pipe, dehydration associated gas escape pipe is also connected with the inlet pipe of water cooler two, and the escape pipe of described electric heater two is also connected to the inlet pipe of water cooler two.
Molecular sieve in described high pressure molecular dehydration adsorption tower C and high pressure molecular dehydration regenerator column D is 4A type molecular sieve or 5A type molecular sieve.
The shallow cold mixing cryogen in described LPG ice chest stage adopts LPG, LPG to enter LPG ice chest by refrigerant compressor supercharging after overflash, dehydration, and after pre-cooled, reducing pressure by regulating flow forms shallow cold mixing cryogen.
The deep cooling azeotrope in described LNG ice chest stage adopts LPG and liquid nitrogen, liquid nitrogen enters LNG ice chest by refrigerant compressor supercharging after overflash, LPG also enters LPG ice chest by refrigerant compressor supercharging after overflash, dehydration, and LPG and nitrogen reducing pressure by regulating flow after pre-cooled forms deep cooling azeotrope.
The beneficial effects of the utility model:
1. have employed Dewatering technology, every one-level dehydration indexes meets corresponding processing requirement;
2. adopt the dewatering process of high-low pressure, each has oneself feature and subject range;
3. in the lower pressure stage that dehydrating amount is large, sorbent material made by the 3A molecular sieve that have employed low porosity, only to dehydration effectively; In high pressure essence dehydration stages, owing to not having the impact of heavy hydrocarbon, the molecular sieve pores porosity increased, while raising dehydrating effect, also can check on for the last time to CO2, H2S and remove.
4. resurgent gases make use of high pressure essence dehydration after purification lean gas, ensure that the quality of resurgent gases to greatest extent;
5. adopt thermal oil and electrically heated combined heated pattern, take full advantage of existing heating system, improve the reliability of heating.
6. inter-stage resurgent gases does not cool, is not separated, and secondary reheats, energy-saving and cost-reducing, simple flow.
Accompanying drawing explanation
Below with reference to accompanying drawing, the utility model is described in further details.
Fig. 1 is total technological process schematic diagram of the present utility model.
Fig. 2 is dehydration technology process flow diagram.
Fig. 3 is high pressure dehydration process schematic diagram.
Description of reference numerals: 1, the first gas-liquid separator; 2, stage compressor; 3, the second gas-liquid separator; 4, dehydration technology sled; 5, solid method fine de-sulfur equipment; 6, two stage compressor; 7, the 3rd gas-liquid separator; 8, LPG ice chest; 9, heavy hydrocarbon washing tower; 10, heavy hydrocarbon deethanizing column; 11, mixed hydrocarbon debutanizing tower; 12, high press-dehydrating sled; 13, LNG ice chest; 14, denitrogenation stripping tower; 15, resurgent gases goes dehydration technology to export; 16, resurgent gases is from high press-dehydrating entrance; 17, water cooler one; 18, electric heater one; 19, unstripped gas strainer one; 20, water separator; 21, interchanger one; 22, dust filter unit one; 23, water cooler two; 24, electric heater two; 25, unstripped gas strainer two; 26, interchanger two; 27, dust filter unit two; 28, demercuration tower.
Embodiment
Embodiment 1:
The present embodiment provides a kind of saturated aqueous oil field gas to reclaim the comprehensive smart dewatering system of LNG/LPG/NGL product, as shown in Figure 1, comprises raw material associated gas pressurizing and clean unit, LPG cold box unit, heavy hydrocarbon fractionation unit and LPG cold box unit.
Raw material associated gas pressurizing and clean unit are prized 4 by the first gas-liquid separator 1 connected successively, stage compressor 2, second gas-liquid separator 3, desulfurization and decarburization device and dehydration technology and are formed.
LPG cold box unit is made up of solid method fine de-sulfur equipment 5, two stage compressor 6, the 3rd gas-liquid separator 7, LPG ice chest 8, Gu method fine de-sulfur equipment 5 is connected to dehydration technology sled 4, Gu method fine de-sulfur equipment 5, two stage compressor 6, the 3rd gas-liquid separator 7 connect successively, the outlet line of the 3rd gas-liquid separator 7 is through LPG ice chest 8.
Heavy hydrocarbon fractionation unit comprises heavy hydrocarbon washing tower 9, heavy hydrocarbon deethanizing column 10, mixed hydrocarbon debutanizing tower 11 and high press-dehydrating sled 12, the outlet line of described 3rd gas-liquid separator 7 is communicated with heavy hydrocarbon washing tower 9 after LPG ice chest 8, the tower bottom outlet pipeline of heavy hydrocarbon washing tower 9 is communicated with heavy hydrocarbon deethanizing column 10, the tower top outlet pipeline of heavy hydrocarbon deethanizing column 10 exports as methane rich overhead gas after LPG ice chest 8, the tower bottom outlet pipeline of heavy hydrocarbon deethanizing column 10 connects mixed hydrocarbon debutanizing tower 11, the tower top outlet of mixed hydrocarbon debutanizing tower 11 is LPG outlet, the tower bottom outlet of mixed hydrocarbon debutanizing tower 11 is NGL outlet, the tower top outlet pipeline of heavy hydrocarbon washing tower 9 is communicated with high press-dehydrating sled 12 after LPG ice chest 8.
LPG cold box unit comprises LNG ice chest 13 and denitrogenation stripping tower 14, the outlet line of described high press-dehydrating sled 12 is by being communicated to denitrogenation stripping tower 14 after LNG ice chest 13, the tower top outlet of denitrogenation stripping tower 14 is rich nitrogen offgas outlet, and the tower bottom outlet pipeline of denitrogenation stripping tower 14 is again by being communicated to LNG storage tank after LNG ice chest 13.
The technology process process of the comprehensive smart dewatering system of this saturated aqueous oil field gas recovery LNG/LPG/NGL product of the present embodiment comprises the steps:
Raw material associated gas pressurizing and cleansing phase: external source associated gas of standing is introduced into the first gas-liquid separator 1 and removes soiling solution in gas, then enter stage compressor 2 and carry out supercharging, gas after supercharging is after the second gas-liquid separator 3 carries out decontaminating liquid, enter desulfurization and decarburization device and carry out desulfurization and decarburization technique, the associated gas after desulfurization enters dehydration technology sled 4 and carries out the dehydration of first order molecular sieve;
The LPG ice chest stage:
Associated gas enters solid method fine de-sulfur equipment 5 after one-level dehydration, Gu associated gas enters two stage compressor 6 and carries out supercharging again after method desulfurization, after supercharging, desulfurization associated gas is through the 3rd gas-liquid separator 7, after being separated, associated gas enters LPG ice chest 8, in LPG ice chest 8 after shallow cold mixing cryogen cooling, enter heavy hydrocarbon washing tower 9;
Heavy hydrocarbon fractionation stage: after heavy hydrocarbon washing tower 9, is divided into low temperature lime set at the bottom of tower and tower top combination gas two-way;
At the bottom of tower, low temperature lime set enters heavy hydrocarbon deethanizing column 10, and after heavy hydrocarbon deethanizing column 10, be divided into the low mixed hydrocarbon two-way containing the first and second alkane at the bottom of tower top methane-rich gas and tower, tower top methane-rich gas, after LPG ice chest 8 re-heat, collects tower top methane-rich gas; A part enters fuel gas system as fuel gas, and remainder carries out circulation and stress as the incoming stock associated gas pressurizing unit of circulation gas; At the bottom of tower, the low mixed hydrocarbon containing the first and second alkane enters mixed hydrocarbon debutanizing tower 11, at the bottom of the tower top and tower of mixed hydrocarbon debutanizing tower 11, collect gas phase LPG and liquid phase NGL respectively;
Tower top combination gas again enters high pressure dehydration sled 12 and carries out secondary molecules sieve deep dehydration after LPG ice chest 8 cools;
The LNG ice chest stage:
The Sweet natural gas going out LPG ice chest enters secondary molecules sieve deep dehydration, then LNG ice chest 13 is entered, denitrogenation stripping tower 14 is entered after the cooling of deep cooling azeotrope, obtain rich nitrogen tail gas raw material as deep cooling azeotrope after the re-heat of LNG ice chest from denitrogenation stripping tower 14 tower top, liquid phase LNG at the bottom of denitrogenation stripping tower 14 tower enters LNG storage tank accumulating as LNG product again after LNG ice chest 13 cools.
In a word, the top gaseous phase (LPG) of mixed hydrocarbon debutanizing tower 11 through refrigerated separation rear section as phegma blowback tower top, remainder as LPG product pump to accumulating unit.The NGL product introduction accumulating unit the most after cooling of liquid phase (NGL) at the bottom of the tower of mixed hydrocarbon debutanizing tower 11; The rich nitrogen tail gas of denitrogenation stripping tower 14 tower top after the re-heat of LNG ice chest as the raw material of deep cooling azeotrope, liquid phase LNG at the bottom of tower removes accumulating unit as LNG product after LNG ice chest cools again, finally realizes the comprehensive essence dehydration that saturated aqueous oil field gas reclaims LNG/LPG/NGL product.
Embodiment 2:
Being provided with resurgent gases in high press-dehydrating sled 12 goes dehydration technology to export 15, is provided with resurgent gases from high press-dehydrating entrance 16 in described dehydration technology sled 4, and resurgent gases connects resurgent gases from high press-dehydrating entrance 16 and goes dehydration technology to export 15.
As shown in Figure 2, described dehydration technology sled 4 comprises low pressure molecular dehydration adsorption tower A, low pressure molecular dehydration regenerator column B, water cooler 1 and electric heater 1;
The tower top fairlead of low pressure molecular dehydration adsorption tower A and low pressure molecular dehydration regenerator column B is divided into two-way, leads up to valve A1, B1 to be connected with low pressure associated gas inlet pipe, separately leads up to valve A2, B2 to be connected with the inlet pipe of water cooler 1; Described low pressure associated gas inlet pipe is provided with a unstripped gas strainer 1, and the escape pipe of described water cooler 1 is connected to water separator 20 inlet pipe, and the escape pipe of water separator 20 is connected to unstripped gas strainer 1 inlet pipe;
The tower reactor fairlead of low pressure molecular dehydration adsorption tower A and low pressure molecular dehydration regenerator column B is also divided into two-way, leading up to valve A3, B3 is connected with dehydration associated gas escape pipe, separately leading up to valve A4, B4 is connected with the escape pipe of electric heater 1, and the inlet mouth of electric heater 1 is communicated with the air outlet of interchanger 1; Described dehydration associated gas escape pipe is provided with a dust filter unit 1, the inlet mouth of described interchanger 1 connects resurgent gases from high press-dehydrating entrance 16, resurgent gases is also connected with the inlet pipe of water cooler 1 from high press-dehydrating entrance 16, and the escape pipe of described electric heater 1 is also connected to the inlet pipe of water cooler 1.
This low-pressure molecular sieve dehydration of the present embodiment, associated gas through wet desulphurization decarburization enters low-pressure molecular sieve dehydration, adopt double tower pattern, 1 tower absorption, another 1 tower regeneration, arranges unstripped gas and filters, avoid free liquid to enter molecular sieve before absorption, after absorption, dust filter unit is set, avoids sieve particle to enter next stage unit.Adopt high-pressure regeneration moisture step-down thermal regeneration, adopt water-cooled to be separated, the associated gas after dehydration goes solid method fine de-sulfur equipment to carry out fine de-sulfur.
Embodiment 3:
As shown in Figure 3, described high press-dehydrating sled 12 comprises high pressure molecular dehydration adsorption tower C, high pressure molecular dehydration regenerator column D, water cooler 2 23 and electric heater 2 24;
The tower top fairlead of high pressure molecular dehydration adsorption tower C and high pressure molecular dehydration regenerator column D is divided into two-way, leads up to valve C1, D1 to be connected with high pressure associated gas inlet pipe, separately leads up to valve C2, D2 to be connected with the inlet pipe of water cooler 2 23; Described high pressure associated gas inlet pipe is provided with a unstripped gas strainer 2 25, and the escape pipe of described water cooler 2 23 is connected to resurgent gases and goes dehydration technology to export 15;
The tower reactor fairlead of high pressure molecular dehydration adsorption tower C and low pressure molecular dehydration regenerator column D is also divided into two-way, leading up to valve C3, D3 is connected with dehydration associated gas escape pipe, separately leading up to valve C4, D4 is connected with the escape pipe of electric heater 2 24, and the inlet mouth of electric heater 2 24 is communicated with the air outlet of interchanger 2 26; Described dehydration associated gas escape pipe is provided with a dust filter unit 2 27 and a demercuration tower 28, the inlet mouth of described interchanger 2 26 is connected to dehydration associated gas escape pipe, dehydration associated gas escape pipe is also connected with the inlet pipe of water cooler 2 23, and the escape pipe of described electric heater 2 24 is also connected to the inlet pipe of water cooler 2 23.
This high pressure molecular sieve dehydration of the present embodiment, the associated gas taking off heavy hydrocarbon through cold washing enters high pressure molecular sieve dehydration, adopt double tower pattern, 1 tower absorption, another 1 tower regeneration, arranges unstripped gas and filters, avoid free liquid to enter molecular sieve before absorption, demercuration tower and dust filter unit are set after absorption, avoid sieve particle to enter next stage unit.Adopt the regeneration of high pressure purge lean gas, adopt thermal oil and some heating mode, the associated gas after final dewatering goes solid method fine de-sulfur equipment to carry out fine de-sulfur.Resurgent gases in the present embodiment goes dehydration technology to export 15, makes resurgent gases step-down and enters dehydration technology after second-heating, like this will be more fully clean for each gas finally obtained.And in the present embodiment, resurgent gases reheats and have employed thermal oil and electrically heated integrated mode, the potential temperature of full factory thermal oil does not meet heating requirements, when making full use of the heat of thermal oil again, electrically heated is utilized to improve resurgent gases potential temperature, simplify heat-conducting oil heating system, improve the reliability of heating.
Embodiment 4:
Molecular sieve in low pressure molecular dehydration adsorption tower A, low pressure molecular dehydration regenerator column B is 3A type molecular sieve.
Molecular sieve in high pressure molecular dehydration adsorption tower C and high pressure molecular dehydration regenerator column D is 4A type molecular sieve or 5A type molecular sieve.
The quality of regenerating molecular sieve effect determines its adsorption effect, the absorption of high pressure essence needs high-level efficiency to regenerate, resurgent gases can not contain heavy hydrocarbon, water dew point requires high, and low pressure thick absorption regeneration tolerance demand is large, less demanding to water dew point, adopts high and low pressure series-connected regenerative pattern, enters low-pressure molecular sieve again and regenerate after the resurgent gases namely after high-pressure regeneration reheats.
Under low pressure operating mode, the precision of dehydration meets the operating requirement of LPG ice chest, and (temperature is lower, and saturation water air pressure is just less for water dew point.So for the air containing a certain amount of steam,
air pressureconstant situation decline low temperature, makes
saturation vapour pressuretemperature when being down to equal with vapor pressure actual at that time, is called dew point.And when temperature is certain, start from
gas phasein isolate the pressure of first drop, or when pressure is certain, starts the temperature isolating first drop from gas phase, be just called water dew point.) minimumly reach-35 DEG C, under this operating mode, due in associated gas containing a large amount of heavy hydrocarbons, molecular sieve type selects 3A type to be main, avoids adsorbs hydrocarbons component.
Under high pressure operating mode, water dew point must meet the operating requirement of LNG ice chest, reach less than-160 DEG C, under this operating mode, associated gas washs through heavy hydrocarbon, and the content of heavy hydrocarbon reaches below 50ppm, now, molecular sieve type can adopt the composite type of 4A+5A, and 5A molecular sieve can be checked on for the last time to CO2, H2S and be removed; The quality of regenerating molecular sieve effect determines its adsorption effect, the absorption of high pressure essence needs high-level efficiency to regenerate, resurgent gases can not contain heavy hydrocarbon, water dew point requires high, low pressure is slightly adsorbed needs amount of regeneration large, less demanding to water dew point, adopts high and low pressure series-connected regenerative pattern, enters low-pressure molecular sieve again and regenerate after the resurgent gases namely after high-pressure regeneration reheats.
Embodiment 5:
The shallow cold mixing cryogen in LPG ice chest stage adopts LPG, LPG to enter LPG ice chest by refrigerant compressor supercharging after overflash, dehydration, and after pre-cooled, reducing pressure by regulating flow forms shallow cold mixing cryogen.
LPG is in operation in earlier stage all by outsourcing, and after normal operation, the gas phase LPG of the overhead collection of mixed hydrocarbon debutanizing tower 11 also can be used as shallow cold mixing cryogen and uses.
The deep cooling azeotrope in LNG ice chest stage adopts LPG and liquid nitrogen, liquid nitrogen enters LNG ice chest by refrigerant compressor supercharging after overflash, LPG also enters LPG ice chest by refrigerant compressor supercharging after overflash, dehydration, and LPG and nitrogen reducing pressure by regulating flow after pre-cooled forms deep cooling azeotrope.
LPG and liquid nitrogen are being gone into operation in earlier stage all by outsourcing; After normal operation, the gas phase LPG of the overhead collection of mixed hydrocarbon debutanizing tower 11 also can be used as deep cooling azeotrope and uses, and the rich nitrogen tail gas that denitrogenation stripping tower 14 tower top obtains supplements nitrogen loss.Wherein, outsourcing LNG, need to carry out proportioning according to practical situation from the ratio of the gas phase LPG produced and nitrogen, according to required deep cooling degree number decide to need nitrogen number.
In sum, this saturated aqueous oil field gas of the present utility model reclaims the comprehensive smart dewatering system of LNG/LPG/NGL product, for the feature of media components, have employed dissimilar molecular sieve and combines; For different dehydration requirements, have employed high-low pressure series combination dehydration mode, meet the requirement of different water dew point respectively; Have employed high pressure purge lean gas as resurgent gases, series-connected regenerative is carried out to high-low pressure dehydration, avoids the impact of resurgent gases on regeneration effect.Dewatering, thinking is novel, advanced technology, and energy consumption is lower, stable, and it is convenient to safeguard.
More than exemplifying is only illustrate of the present utility model, does not form the restriction to protection domain of the present utility model, everyly all belongs within protection domain of the present utility model with the same or analogous design of the utility model.
Claims (8)
1. saturated aqueous oil field gas reclaims a comprehensive smart dewatering system for LNG/LPG/NGL product, it is characterized in that: comprise raw material associated gas pressurizing and clean unit, LPG cold box unit, heavy hydrocarbon fractionation unit and LPG cold box unit,
Described raw material associated gas pressurizing and clean unit are prized (4) by the first gas-liquid separator (1) connected successively, stage compressor (2), the second gas-liquid separator (3), desulfurization and decarburization device and dehydration technology and are formed;
Described LPG cold box unit is made up of solid method fine de-sulfur equipment (5), two stage compressor (6), the 3rd gas-liquid separator (7), LPG ice chest (8), Gu method fine de-sulfur equipment (5) is connected to dehydration technology sled (4), Gu method fine de-sulfur equipment (5), two stage compressor (6), the 3rd gas-liquid separator (7) connect successively, the outlet line of the 3rd gas-liquid separator (7) is through LPG ice chest (8);
Described heavy hydrocarbon fractionation unit comprises heavy hydrocarbon washing tower (9), heavy hydrocarbon deethanizing column (10), mixed hydrocarbon debutanizing tower (11) and high press-dehydrating sled (12), the outlet line of described 3rd gas-liquid separator (7) is communicated with heavy hydrocarbon washing tower (9) after LPG ice chest (8), the tower bottom outlet pipeline of heavy hydrocarbon washing tower (9) is communicated with heavy hydrocarbon deethanizing column (10), the tower top outlet pipeline of heavy hydrocarbon deethanizing column (10) exports as methane rich overhead gas after LPG ice chest (8), the tower bottom outlet pipeline of heavy hydrocarbon deethanizing column (10) connects mixed hydrocarbon debutanizing tower (11), the tower top outlet of mixed hydrocarbon debutanizing tower (11) is LPG outlet, the tower bottom outlet of mixed hydrocarbon debutanizing tower (11) is NGL outlet, the tower top outlet pipeline of heavy hydrocarbon washing tower (9) is communicated with high press-dehydrating sled (12) after LPG ice chest (8),
Described LPG cold box unit comprises LNG ice chest (13) and denitrogenation stripping tower (14), the outlet line of described high press-dehydrating sled (12) is communicated to denitrogenation stripping tower (14) by after LNG ice chest (13), the tower top outlet of denitrogenation stripping tower (14) is rich nitrogen offgas outlet, and the tower bottom outlet pipeline of denitrogenation stripping tower (14) is communicated to LNG storage tank by after LNG ice chest (13) again.
2. saturated aqueous oil field gas as claimed in claim 1 reclaims the comprehensive smart dewatering system of LNG/LPG/NGL product, it is characterized in that: be provided with resurgent gases in described high press-dehydrating sled (12) and go dehydration technology to export (15), be provided with resurgent gases from high press-dehydrating entrance (16) in described dehydration technology sled (4), resurgent gases connects resurgent gases from high press-dehydrating entrance (16) and goes dehydration technology to export (15).
3. saturated aqueous oil field gas as claimed in claim 1 reclaims the comprehensive smart dewatering system of LNG/LPG/NGL product, it is characterized in that: described dehydration technology sled (4) comprises low pressure molecular dehydration adsorption tower (A), low pressure molecular dehydration regenerator column (B), water cooler one (17) and electric heater one (18);
Described low pressure molecular dehydration adsorption tower (A) and the tower top fairlead of low pressure molecular dehydration regenerator column (B) are divided into two-way, valve (A1, B1) of leading up to is connected with low pressure associated gas inlet pipe, and valve (A2, B2) of separately leading up to is connected with the inlet pipe of water cooler one (17); Described low pressure associated gas inlet pipe is provided with a unstripped gas strainer one (19), the escape pipe of described water cooler one (17) is connected to water separator (20) inlet pipe, and the escape pipe of water separator (20) is connected to unstripped gas strainer one (19) inlet pipe;
Described low pressure molecular dehydration adsorption tower (A) and the tower reactor fairlead of low pressure molecular dehydration regenerator column (B) are also divided into two-way, valve (A3, B3) of leading up to is connected with dehydration associated gas escape pipe, valve (A4, B4) of separately leading up to is connected with the escape pipe of electric heater one (18), and the inlet mouth of electric heater one (18) is communicated with the air outlet of interchanger one (21); Described dehydration associated gas escape pipe is provided with a dust filter unit one (22), the inlet mouth of described interchanger one (21) connects resurgent gases from high press-dehydrating entrance (16), resurgent gases is also connected with the inlet pipe of water cooler one (17) from high press-dehydrating entrance (16), and the escape pipe of described electric heater one (18) is also connected to the inlet pipe of water cooler one (17).
4. saturated aqueous oil field gas as claimed in claim 3 reclaims the comprehensive smart dewatering system of LNG/LPG/NGL product, it is characterized in that: the molecular sieve in described low pressure molecular dehydration adsorption tower (A), low pressure molecular dehydration regenerator column (B) is 3A type molecular sieve.
5. the saturated aqueous oil field gas as described in Claims 2 or 3 or 4 reclaims the comprehensive smart dewatering system of LNG/LPG/NGL product, it is characterized in that: described high press-dehydrating sled (12) comprises high pressure molecular dehydration adsorption tower (C), high pressure molecular dehydration regenerator column (D), water cooler two (23) and electric heater two (24);
Described high pressure molecular dehydration adsorption tower (C) and the tower top fairlead of high pressure molecular dehydration regenerator column (D) are divided into two-way, valve (C1, D1) of leading up to is connected with high pressure associated gas inlet pipe, and valve (C2, D2) of separately leading up to is connected with the inlet pipe of water cooler two (23); Described high pressure associated gas inlet pipe is provided with a unstripped gas strainer two (25), and the escape pipe of described water cooler two (23) is connected to resurgent gases and goes dehydration technology to export (15);
Described high pressure molecular dehydration adsorption tower (C) and the tower reactor fairlead of low pressure molecular dehydration regenerator column (D) are also divided into two-way, valve (C3, D3) of leading up to is connected with dehydration associated gas escape pipe, valve (C4, D4) of separately leading up to is connected with the escape pipe of electric heater two (24), and the inlet mouth of electric heater two (24) is communicated with the air outlet of interchanger two (26); Described dehydration associated gas escape pipe is provided with a dust filter unit two (27) and a demercuration tower (28), the inlet mouth of described interchanger two (26) is connected to dehydration associated gas escape pipe, dehydration associated gas escape pipe is also connected with the inlet pipe of water cooler two (23), and the escape pipe of described electric heater two (24) is also connected to the inlet pipe of water cooler two (23).
6. saturated aqueous oil field gas as claimed in claim 5 reclaims the comprehensive smart dewatering system of LNG/LPG/NGL product, it is characterized in that: the molecular sieve in described high pressure molecular dehydration adsorption tower (C) and high pressure molecular dehydration regenerator column (D) is 4A type molecular sieve or 5A type molecular sieve.
7. saturated aqueous oil field gas as claimed in claim 1 reclaims the comprehensive smart dewatering system of LNG/LPG/NGL product, it is characterized in that: the shallow cold mixing cryogen in described LPG ice chest stage adopts LPG, LPG enters LPG ice chest by refrigerant compressor supercharging after overflash, dehydration, and after pre-cooled, reducing pressure by regulating flow forms shallow cold mixing cryogen.
8. saturated aqueous oil field gas as claimed in claim 1 reclaims the comprehensive smart dewatering system of LNG/LPG/NGL product, it is characterized in that: the deep cooling azeotrope in described LNG ice chest stage adopts LPG and liquid nitrogen, liquid nitrogen enters LNG ice chest by refrigerant compressor supercharging after overflash, LPG also enters LPG ice chest by refrigerant compressor supercharging after overflash, dehydration, and LPG and nitrogen reducing pressure by regulating flow after pre-cooled forms deep cooling azeotrope.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108998131A (en) * | 2018-10-22 | 2018-12-14 | 西南石油大学 | A kind of high sulfur Gas Fields gathering system high-efficiency desulfurization, dehydration device and method |
| CN112745974A (en) * | 2020-12-14 | 2021-05-04 | 中海石油(中国)有限公司 | Membrane separation method oilfield associated gas purification process and system based on adsorption dehydration pretreatment |
| CN112812806A (en) * | 2021-02-04 | 2021-05-18 | 四川杰瑞恒日天然气工程有限公司 | Process and system for producing light hydrocarbon and LNG (liquefied Natural gas) from oilfield associated gas |
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- 2015-08-28 CN CN201520659080.1U patent/CN205011721U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108998131A (en) * | 2018-10-22 | 2018-12-14 | 西南石油大学 | A kind of high sulfur Gas Fields gathering system high-efficiency desulfurization, dehydration device and method |
| CN108998131B (en) * | 2018-10-22 | 2023-12-08 | 西南石油大学 | High-efficiency desulfurization and dehydration device and method for high-sulfur-content gas field gathering and transportation system |
| CN112745974A (en) * | 2020-12-14 | 2021-05-04 | 中海石油(中国)有限公司 | Membrane separation method oilfield associated gas purification process and system based on adsorption dehydration pretreatment |
| CN112812806A (en) * | 2021-02-04 | 2021-05-18 | 四川杰瑞恒日天然气工程有限公司 | Process and system for producing light hydrocarbon and LNG (liquefied Natural gas) from oilfield associated gas |
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