CN205258018U - Gas field carbon dioxide preparation industry liquid carbon dioxide separation and purification system - Google Patents
Gas field carbon dioxide preparation industry liquid carbon dioxide separation and purification system Download PDFInfo
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- CN205258018U CN205258018U CN201521055976.5U CN201521055976U CN205258018U CN 205258018 U CN205258018 U CN 205258018U CN 201521055976 U CN201521055976 U CN 201521055976U CN 205258018 U CN205258018 U CN 205258018U
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Abstract
The utility model discloses a gas field carbon dioxide preparation industry liquid carbon dioxide separation and purification system is mainly carried by well head separating element (1), reboiling distillation unit (2), condensation liquefaction unit (3), absorption regenerating unit (4), high pressure and heats up in a steamer unit (5) and store pressure boost unit (6) and form. The gas -liquid export and distillation reboiler (21) the pipeline connection of well head separating element (1), gas exports and distillation column (22) of distillation reboiler (21), the gaseous phase entry of adsorption tower (41), the lower part gas exports of adsorption tower (41) and the middle part gaseous phase entry of carbon dioxide condenser (51), the liquid phase export and the high pressure of carbon dioxide condenser (51) are carried the liquid phase entry that heats up in a steamer tower (52) and are passed through pipeline end -to -end connection in proper order, the high pressure is put forward the lower part liquid phase of heating up in a steamer tower (52) and is exported through finished product pans (61) and carbon dioxide storage tank (63) pipeline connection. This system prepares industry liquid carbon dioxide purity and is higher than 99.9%.
Description
Technical field
The utility model relates to carbon dioxide separation purification technique field, especially relates to the carbon dioxide preparation of a kind of gas fieldIndustrial liquid carbon dioxide separation purification system.
Background technology
Carbon dioxide is widely used in welding, chemical industry, food, the oil field displacement of reservoir oil and engineering science and technology technical field. According to existing stateFamily's standard (GB/T6052-2011 industrial liquid carbon dioxide) and professional standard (HG/T2537--1993) regulation, industrialIts purity of liquid CO 2 reaches more than 99%, and free water, oil content must not detect, free from extraneous odour, its purity of carbon dioxide for weldingReach more than 99.5%, below moisture content 50ppm, aqueous water, oil content must not detect, and free from extraneous odour, in order to meet industrial liquid carbon dioxideCountry's use standard, must carry out separating-purifying to gas field carbon dioxide. Current existing carbon dioxide purification technique mainly containsChemistry, Physical Absorption method, absorption method, low temperature processing, membrane separation process etc. But the main pin of existing several processing methods at presentThe unstripped gas such as chemical industry tail gas, flue gas is purified, and energy consumption is high, treating capacity is little, product design is low, for high pressure, large reservesGas field carbon dioxide inapplicable, therefore, urgently research and develop one and give vent to anger as raw material for carbon dioxide gas real estate speciallyCarbon dioxide separation method of purification.
Utility model content
The purpose of this utility model is to overcome the deficiency in existing carbon dioxide purification separator and technology, provides" a kind of gas field carbon dioxide is prepared industrial liquid carbon dioxide separation purification system ", the utility model mainly adopts unstripped gasCrude separation, distillation, condensation liquefaction, absorption regeneration, high pressure are carried and are heated up in a steamer, store supercharging purification technique, collection absorption method, low temperature processing andHigh pressure is put forward the technology of heating up in a steamer in one. This system structure design, connection, rationally distributed, cost is low, makes full use of the native system energy, jointCan lower consumption, realize gas field carbon dioxide and prepare the large-scale production of industrial liquid carbon dioxide. Prepared industrial liquid titanium dioxideCarbon products purity is higher than 99.9%, and moisture content dew point, lower than-65 DEG C, without free water and oil content, meets country, industry relevant criterion ruleFixed, can be widely used in the fields such as carbon dioxide welding protection gas, industrial chemicals, the oil field pressure injection displacement of reservoir oil.
For achieving the above object, technical solution adopted in the utility model is: main technical scheme is, a kind of gas fieldCarbon dioxide is prepared industrial liquid carbon dioxide separation purification system, mainly by well head separative element 1, reboiled distillation unit 2, coldSolidifying liquefaction unit 3, absorption regeneration unit 4, high pressure are carried heating up in a steamer unit 5 and storing compress cell 6 and are formed. Described well head separative element 1Gas liquid outlet is connected with the gas-liquid suction line of distillation reboiler 21, distill the gaseous phase outlet of reboiler 21 and destilling tower 22The bottom gas phase of the top gaseous phase outlet of middle and lower part gas phase entrance, destilling tower 22 and the gas phase entrance of adsorption tower 41, adsorption tower 41The middle part gas phase entrance of outlet and carbon dioxide condenser 51, the liquid-phase outlet of carbon dioxide condenser 51 and high pressure are carried and are heated up in a steamer tower 52Liquid phase entrance by pipeline successively head and the tail connect, high pressure is carried the bottom liquid-phase outlet that heats up in a steamer tower 52 through finished product pans 61 and dioxyChanging carbon storage tank 63 pipelines connects.
Further technical scheme is that described well head separative element 1 is by well head 11, well head separator 12, sewage disposalPond 13 and pressure-reducing valve I composition. Under in the material outlet of described well head 11 and well head separator 12 entrances, well head separator 12Portion's gas liquid outlet is connected by pipeline successively head and the tail with the entrance of pressure-reducing valve I 14, and well head separator 12 bottom outlets of sewer are with dirtyWater treating pond 13 pipelines connect.
Further technical scheme is, described reboiled distillation unit 2 is by distillation reboiler 21, ammonia helical-lobe compressor 212,Destilling tower 22, carbon dioxide carburettors 23, reflux pump 24 and oil water separator 25 form. Described distillation reboiler 21 respectivelyWith gas liquid outlet, ammonia helical-lobe compressor 212 outputs, the middle and lower part gas phase entrance of destilling tower 22,22 ends of destilling tower of pressure-reducing valve IThe liquid phase suction line at portion's liquid phase carbon dioxide outlet and carbon dioxide carburettors 23 middle parts connects. Described carbon dioxide carburettors23 also export and regeneration gas heat exchanger 42 suction lines are connected with oil water separator 25 entrances, outlet surge tank 67 respectively.
Further technical scheme is that described condensation liquefaction unit 3 is by phegma condenser 31, phegma pans 32Composition. Destilling tower 22 top gaseous phase outlet phegmas are connected with phegma condenser 31 entrances, the liquid of phegma condenser 31Outlet is connected with phegma pans 32, reflux pump 24 and destilling tower 22 upper entrance head and the tail pipelines successively mutually.
Further technical scheme is, described absorption regeneration unit 4 is by adsorption tower 41, regeneration gas heat exchanger 42, regenerationHot-air heater 421 and conduction oil cooler 47 form. Described regeneration gas heat exchanger 42 gaseous phase outlets and regeneration gas heater 421Upper end gas phase entrance connects, and 41 times bottoms of regeneration gas heater 421 upper end gaseous phase outlets and adsorption tower are connected, adsorption tower 41 topsGaseous phase outlet be connected with conduction oil cooler 47 following sides.
Further technical scheme is, described high pressure is carried and heated up in a steamer unit 5 and comprise that carbon dioxide condenser 51, high pressure are carried and heat up in a steamer tower 52And carry and heat up in a steamer tower reboiler 53. The liquid-phase outlet of described carbon dioxide condenser 51 and high pressure are carried the liquid phase inlet tube that heats up in a steamer tower 52 middle partsLine connects, and high pressure is carried the bottom side liquid-phase outlet that heats up in a steamer tower 52 through finished product pans 61 and pressure-reducing valve II 62 and carbon dioxide storage tank 63Pipeline connects. Carry and heat up in a steamer the bottom inlet of tower reboiler 53 and high pressure and carry and heat up in a steamer tower 52 outlet at bottoms, carry the top of heating up in a steamer tower reboiler 53Outlet and high pressure carry heat up in a steamer tower 52 middle and lower part entrance, carry heat up in a steamer tower reboiler 53 entry and exit, middle part respectively with adsorption tower 41 entrancesBe connected with regeneration gas heat exchanger 42 outlet lines.
Further technical scheme is that described storage compress cell 6 comprises carbon dioxide storage tank 63, suction port of compressor heat exchangeDevice 64 and carbon-dioxide gas compressor 66. The gaseous phase outlet of described carbon dioxide storage tank 63 successively through compressor entrance heat exchanger 64,Inlet buffer 65, carbon-dioxide gas compressor 66, outlet surge tank 67, carbon dioxide carburettors 23 are managed with regeneration gas heat exchanger 42Line connects.
Further technical scheme is, described adsorption tower 41 is set to one and opens one for Double-Tower Structure, and destilling tower 22 passes through lockValve I is connected with adsorption tower I and adsorption tower II top entrance respectively with gate valve II, and the lower bottom of adsorption tower I and adsorption tower II is through lockAfter being connected in parallel with gate valve IV, valve III is connected with carbon dioxide condenser 51 entrances.
The utility model compared with prior art tool has the following advantages:
1, the utility model mainly adopts unstripped gas crude separation, distillation, condensation liquefaction, absorption regeneration, high pressure to carry to heat up in a steamer, storeSupercharging purification technique, integrates absorption method, low temperature processing and high pressure and puies forward the technology of heating up in a steamer. This system structure design, connection, layoutRationally, cost is low, makes full use of the native system energy, energy-saving and cost-reducing, realizes gas field carbon dioxide and prepares industrial liquid carbon dioxideLarge-scale production. Prepared industrial liquid carbon dioxide purity, higher than 99.9%, meets state-set standard, can be widely used inThe fields such as carbon dioxide welding protection gas, industrial chemicals, the oil field pressure injection displacement of reservoir oil.
2, carry and heat up in a steamer, store up because the utility model adopts unstripped gas crude separation, reboiled distillation, condensation liquefaction, absorption regeneration, high pressureDeposit supercharging purification technique, make full use of feature and the character of various facility separating-purifyings, collection absorption method, low temperature processing and high pressurePut forward the technology of heating up in a steamer in one, guarantee that the liquid CO 2 that enters carbon dioxide storage tank is higher than 99.9%, moisture content dew point is lower than-65 DEG C,Without free water and oil content, meet country, industry correlation standard, can be widely used in carbon dioxide welding protection gas, chemical industryThe fields such as raw material, the oil field pressure injection displacement of reservoir oil.
3, open one for Double-Tower Structure because adsorption tower 41 is set to one, double tower adsorbs in turn, regenerates, not only safe but also efficient.
4,, because being provided with carbon-dioxide gas compressor, utilize carbon-dioxide gas compressor by the gaseous state dioxy in carbon dioxide storage tankChange carbon and draw back, not only make pressure of storage tank controlled and further improve the quality of products, the carbon dioxide after compression obtains higherTemperature rise, enter the tube side of carbon dioxide carburettors after surge tank through outlet, carry out after heat exchange with the profit carbon dioxide of shell sideThrough regeneration gas heat exchanger with carry and heat up in a steamer reboiler and enter adsorption tower entrance, realize repeatedly recycling and the storage tank gas phase dioxy of heatChange the further separating-purifying of carbon.
Brief description of the drawings
Fig. 1 is structural representation of the present utility model.
Fig. 2 is distillation unit connection structure schematic diagram of the present utility model.
Fig. 3 is that in absorption regeneration of the present utility model unit, adsorption tower arranges structural representation.
Fig. 4 is absorption regeneration unit connection structure schematic diagram of the present utility model.
Fig. 5 is that high pressure of the present utility model is carried and heated up in a steamer unit connection structure schematic diagram.
In figure: 1, well head separative element, 11, well head, 12, well head separator, 13, treatment tank, 14, pressure-reducing valve I, 2,Reboiled distillation unit, 21, distillation reboiler, 211, storage ammonia tank, 212, ammonia helical-lobe compressor, 22, destilling tower, 23, carbon dioxideVaporizer, 231, vent line, 24, reflux pump, 25, oil water separator, 3, condensation liquefaction unit, 31, phegma condenser,32, phegma pans, 4, absorption regeneration unit, 41, adsorption tower, 411, adsorption tower I, 412, adsorption tower II, 413, tail gas rowBlank pipe line, 42, regeneration gas heat exchanger, 421, regeneration gas heater, 43, gate valve I, 44, gate valve II, 45, gate valve III, 46, gate valveIV, 47, conduction oil cooler, 471, conduction oil intake pipeline, 472, conduction oil export pipeline, 473, coolant intake pipe line,474, coolant outlet hose line, 5, high pressure carries and heat up in a steamer unit, 51, carbon dioxide condenser, 511, ammonia intake pipeline, 52, high pressure carriesHeat up in a steamer tower, 53, carry and heat up in a steamer tower reboiler, 6, store compress cell, 61, finished product pans, 62, pressure-reducing valve II, 63, carbon dioxide storageTank, 64, suction port of compressor heat exchanger, 65, inlet buffer, 66, carbon-dioxide gas compressor, 67, outlet surge tank, 7, total for ammoniaPipe.
Detailed description of the invention
Below in conjunction with accompanying drawing, by non-limiting example, the utility model is described in further detail.
Embodiment
This gas field carbon dioxide is prepared industrial liquid carbon dioxide separation purification system as shown in Figure 1, is mainly divided by well headFrom unit 1, reboiled distillation unit 2, condensation liquefaction unit 3, absorption regeneration unit 4, high pressure carry and heat up in a steamer unit 5 and store compress cell6 compositions. The gas liquid outlet of described well head separative element 1 is connected with the gas-liquid suction line of distillation reboiler 21, distillation reboilerMiddle and lower part gas phase entrance, the top gaseous phase outlet of destilling tower 22 and the gas phase of adsorption tower 41 of 21 gaseous phase outlet and destilling tower 22The middle part gas phase entrance of the bottom gaseous phase outlet of entrance, adsorption tower 41 and carbon dioxide condenser 51, carbon dioxide condenser 51Liquid-phase outlet and high pressure carry the liquid phase entrance that heats up in a steamer tower 52 and be connected by pipeline successively head and the tail, high pressure is put forward the bottom liquid phase of heating up in a steamer tower 52Outlet is connected with carbon dioxide storage tank 63 pipelines through finished product pans 61.
Described well head separative element 1 is made up of well head 11, well head separator 12, treatment tank 13 and pressure-reducing valve I 14. The feed carbon dioxide pressure of well head 11 is more than 6.5MPa, and feed carbon dioxide is inputted to well head separator 12, and well head dividesBe connected the 12 bottom dirts of well head separator by pipeline successively head and the tail from the middle and lower part gas liquid outlet of device 12 and the entrance of pressure-reducing valve IWater out is connected with treatment tank 13 pipelines.
As shown in Figure 1 and Figure 2, described reboiled distillation unit 2 is by distillation reboiler 21, ammonia helical-lobe compressor 212, distillationTower 22, carbon dioxide carburettors 23, reflux pump 24 and oil water separator 25 form. Described distillation reboiler 21 respectively with subtractThe gas liquid outlet of pressure valve I, ammonia helical-lobe compressor 212 outputs, the middle and lower part gas phase entrance of destilling tower 22, destilling tower 22 bottom liquidThe water inlet pipeline at the outlet of phase carbon dioxide and carbon dioxide carburettors 23 middle parts connects. Described carbon dioxide carburettors 23 also dividesNot with oil water separator 25 entrances, export that surge tank 67 exports and regeneration gas heat exchanger 42 suction lines are connected. Carbon dioxide vapourChanging device 23 needs emptying material emptying through vent line 231, and ammonia is through inputting phegma condenser 31 for ammonia house steward 7.
As shown in Figure 1, described condensation liquefaction unit 3 is made up of phegma condenser 31, phegma pans 32. SteamHeat up in a steamer tower 22 tops wherein a road gaseous phase outlet be connected with phegma condenser 31 entrances, the liquid-phase outlet of phegma condenser 31 is complied withInferior and phegma pans 32, reflux pump 24 and destilling tower 22 upper entrances head and the tail pipelines are connected.
As shown in Fig. 1, Fig. 3, Fig. 4, described absorption regeneration unit 4 is by adsorption tower 41, regeneration gas heat exchanger 42, regeneration gasHeater 421 and conduction oil cooler 47 form. On described regeneration gas heat exchanger 42 gaseous phase outlets and regeneration gas heater 421End gas phase entrance connects, and 41 times bottoms of regeneration gas heater 421 upper end gaseous phase outlets and adsorption tower are connected, adsorption tower 41 topsGaseous phase outlet is connected with conduction oil cooler 47 following sides. Described adsorption tower 41 is set to one and opens one for Double-Tower Structure, destilling tower22 are connected with adsorption tower I and adsorption tower II top entrance respectively with gate valve II by gate valve I, under adsorption tower I and adsorption tower IIBottom is connected with carbon dioxide condenser 51 entrances after gate valve III is connected in parallel with gate valve IV. The tail gas that adsorption tower 41 producesDischarge through tail gas vent line 413. Conduction oil is inputted regeneration gas heater 421 through conduction oil intake pipeline 471, and conduction oil is coolingIn device 47, conduction oil is exported through conduction oil export pipeline 472. In conduction oil cooler 47, the required cooling water of institute is respectively through cooling waterIntake pipeline 473 and 474 input and output of coolant outlet hose line.
As shown in Figure 1, shown in Figure 5, described high pressure is carried and is heated up in a steamer unit 5 and comprise that carbon dioxide condenser 51, high pressure are carried and heat up in a steamer tower 52 and carryHeat up in a steamer tower reboiler 53. The liquid-phase outlet of described carbon dioxide condenser 51 and high pressure are carried the liquid phase suction line company of heating up in a steamer tower 52 middle partsConnect, high pressure is carried the bottom side liquid-phase outlet that heats up in a steamer tower 52 through finished product pans 61 and pressure-reducing valve II 62 and carbon dioxide storage tank 63 pipelinesConnect. Carry and heat up in a steamer the bottom inlet of tower reboiler 53 and high pressure and carry and heat up in a steamer tower 52 outlet at bottoms, carry the top exit that heats up in a steamer tower reboiler 53With high pressure carry heat up in a steamer tower 52 middle and lower part entrance, carry heat up in a steamer tower reboiler 53 entry and exit, middle part respectively with adsorption tower 41 entrances and againAngry heat exchanger 42 outlet lines connect. Carbon dioxide condenser 51 and high pressure are carried and are heated up in a steamer the required ammonia of using of tower 52 through ammonia intake pipeline511 inputs.
As shown in Figure 1, described storage compress cell 6 comprises carbon dioxide storage tank 63, suction port of compressor heat exchanger 64 and twoCarbonoxide compressor 66. The gaseous phase outlet of described carbon dioxide storage tank 63 is successively through compressor entrance heat exchanger 64, entrance bufferingTank 65, carbon-dioxide gas compressor 66, outlet surge tank 67, carbon dioxide carburettors 23 are connected with regeneration gas heat exchanger 42 pipelines.
One. each unit critical piece arranges
(1), well head separative element:
1. well head: the unstripped gas 6.5MPa of carbon dioxide gas well, 25 DEG C;
2, well head separator: gravity cyclone type exocentric structure, technical parameter: design pressure: 8.0MPa design temperature: 50DEG C model: nonstandard;
3, treatment tank: capacity: 30m.
(2) distillation unit:
1, distillation reboiler: technical parameter: design pressure (tube side): 2.5MPa design temperature (tube side): establish for 100 DEG CMeter pressure (shell side): 5.2MPa design temperature (shell side) :-15 DEG C of models: nonstandard;
2, storage ammonia tank: technical parameter: design pressure: 2.5MPa design temperature: 50 DEG C of models: nonstandard;
3, ammonia helical-lobe compressor: technical parameter: refrigerating capacity 630kw motor power (output) 250kW model: KA20CBY;
4, destilling tower: technical parameter: design pressure: 5.2MPa design temperature :-10 DEG C of models: nonstandard;
5, carbon dioxide carburettors: technical parameter: design pressure (tube side): 5.2MPa design temperature (tube side): 100 DEG CDesign pressure (shell side): 5.2MPa design temperature (shell side) :-15 DEG C of models: nonstandard;
6, reflux pump: technical parameter: power 3.7kW model: R85-316H4BM-0204T1B1-B;
7, oil water separator: technical parameter: design pressure: 0.6MPa design temperature: 100 DEG C of models: nonstandard.
(3), condensation liquefaction unit:
1, phegma condenser: technical parameter: design pressure (tube side): 1.8MPa design temperature (tube side) :-18 DEG CDesign pressure (shell side): 5.2MPa design temperature (shell side) :-10 DEG C of models: nonstandard;
2, phegma pans: design pressure: 5.0MPa design temperature: 50 DEG C of models: nonstandard.
(4) absorption regeneration unit:
1, adsorption tower: technical parameter: design pressure (chuck): 0.8MPa design temperature (chuck): 350 DEG C of designs are pressedPower: 5.0MPa design temperature: 50 DEG C of models: nonstandard;
2, regeneration gas heat exchanger: technical parameter: design pressure (tube side): 5.0MPa design temperature (tube side): 100 DEG CDesign pressure (shell side): 2.5MPa design temperature (shell side) :-50 DEG C of models: nonstandard;
3, regeneration gas heater: technical parameter: design pressure (tube side): 0.6MPa design temperature (tube side): 300 DEG CDesign pressure (shell side): 1.0MPa design temperature (shell side): 350 DEG C of models: nonstandard;
4, conduction oil cooler: technical parameter: technical parameter: design pressure (chuck): 0.4MPa design temperature (folderCover): 50 DEG C of design pressures: 1MPa design temperature: 300 DEG C of models: nonstandard.
(5) high pressure is carried and is heated up in a steamer unit:
1, carbon dioxide condenser: design pressure (tube side): 2.5MPa design temperature (tube side) :-10 DEG C of designs are pressedPower (shell side): 5.0MPa design temperature (shell side) :-10 DEG C of models: nonstandard;
2, high pressure is carried and is heated up in a steamer tower: technical parameter: design pressure: 5.5MPa design temperature: 50 DEG C of models: nonstandard;
3, carry and heat up in a steamer tower reboiler: technical parameter: design pressure (tube side): 5.0MPa design temperature (tube side): 50 DEG CDesign pressure (shell side): 5.0MPa design temperature (shell side): 100 DEG C of models: nonstandard.
(6) store compress cell:
1, finished product pans: technical parameter: design pressure: 5.0MPa design temperature: 50 DEG C of models: nonstandard;
2, carbon dioxide storage tank: technical parameter: design pressure: 2.5MPa design temperature :-35 DEG C of models: nonstandard;
3, suction port of compressor heat exchanger: technical parameter: design pressure (tube side): 2.5MPa design temperature (tube side) :-25DEG C design pressure (shell side): 2.5MPa design temperature (shell side): 50 DEG C of models: nonstandard;
4, inlet buffer: technical parameter: design pressure: 2.5MPa design temperature: 50 DEG C of models: nonstandard;
5, carbon-dioxide gas compressor: technical parameter: power of motor 250KW, Q=4.5M3/ min model: LW-4.5/20-48；
6, outlet surge tank: technical parameter: design pressure: 5.0MPa design temperature: 150 DEG C of models: nonstandard.
Two, the native system separating-purifying course of work:
From CO 2 raw material gas (6.5MPa, 25 DEG C, carbon dioxide content 98% left and right, the water content of gas well mouth 110.57%), first enter well head separator 12, by the free water containing in gravity whirlwind method divided gas flow, bottom freeWater enters treatment tank 13 and does harmless treatment; The carbon dioxide of well head separator 12 centre exits is decompressed to through pressure-reducing valve I4.8MPa operating pressure enters destilling tower reboiler 21 shell sides, the carbon dioxide of destilling tower reboiler 21 shell sides by tube side from ammoniaHelical-lobe compressor 212 exports the ammonia heating vaporization of high temperature and seethes with excitement, and high boiling oil, water enter carbon dioxide carburettors by bottom23, then enter oil water separator 25 by vaporizer, profit is separated in oil water separator 25, and condensate enters condensateTank, water does harmless treatment by entering wastewater disposal basin, and the gas phase carbon dioxide in destilling tower reboiler 21 enters destilling tower 22 and entersRow separated.
In destilling tower 22, gaseous carbon dioxide rises step by step along packing layer, and overhead reflux liquid is from packing layer under step by step trayStream, so, in constantly mass transfer and the heat exchange of packing layer surface, gas-liquid carbon dioxide is constantly liquefied or vaporizes, and contains high boilingThe liquid carbon dioxide of profit returns destilling tower reboiler 21 from tower bottom flow, the gaseous state two that contains lower carbon number hydrocarbons and other low boiling impurityCarbonoxide flows out from destilling tower 22 tower tops, and wherein, a part enters phegma condenser 31 and liquefies, through phegma condenserCarbon dioxide after 31 liquefaction enters phegma pans 32, and phegma adopts reflux pump 24 to enter distillation from the re-injection of destilling tower tower topTower 22, another part enters adsorption tower 41, dewaters and adsorbs a small amount of impurity, then enters carbon dioxide condenser 51 and carries out liquidChange. Under the effect of destilling tower, carbon dioxide state becomes 4.5MPa, and 9 DEG C, water content drops to 0.2% left and right by 0.57%.
Destilling tower 22 top carbon dioxide enter and include molecular sieve and active carbon as the adsorption tower 41 of filler, remove gasIn peculiar smell and minor amount of water state become 4.3MPa, 7 DEG C, water content is further reduced to 0.006%. The utility model arranges oneOpen one for two adsorption towers, when the filler in adsorption tower I reach absorption saturated after, by switching gate valve I, gate valve II, gate valve III,Gate valve IV valve group, switches adsorption tower II to normal production status, and adsorption tower I is switched to reproduced state, heats in regeneration gasThe high temperature heat conductive oil that device 421 is interior utilizes heat-conducting oil system is to from reverse logical after carrying the carbon dioxide tail gas that heats up in a steamer tower top and heatingCross adsorption tower I, utilize high temperature carbon dioxide to purge desorption to the filler after saturated, realize the regeneration cycle of adsorption tower fillerUtilize.
Liquid carbon dioxide after carbon dioxide condenser 51 liquefaction enters high pressure and carries and heat up in a steamer tower 52 and further separate and carryPure. Carry and heating up in a steamer in tower 52 at high pressure, carbon dioxide carries out rectifying separation again on packing layer, contains on a small quantity two of incoagulable gasCarbonoxide is emptying from tower top, and liquid carbon dioxide enters finished product pans 61 from tower bottom flow, then enters two after the decompression of pressure-reducing valve IICarbonoxide storage tank 63.
The liquid CO 2 flash distillation of high pressure is to 1.95MPa, enters after carbon dioxide storage tank 63 after-20 DEG C, causes storage tankThe increase of pressure rise and incoagulable gas dividing potential drop in tank. Now utilize carbon-dioxide gas compressor 66 by the gas phase dioxy in tankChange carbon and draw back, can make carbon dioxide storage tank 63 pressure controlled and improve the quality of products. Gaseous state in carbon dioxide storage tank 63Carbon dioxide is introduced into suction port of compressor heat exchanger 64, the liquefied ammonia of atmospheric carbon dioxide and shell entering before inlet buffer 65Carry out heat exchange, the temperature of carbon dioxide raises, and the carbon dioxide after compression obtains higher temperature rise, through outlet bufferingAfter tank 67, enter the tube side of carbon dioxide carburettors 23, carry out entering adsorption tower 41 after heat exchange with the profit carbon dioxide of shell side and enterMouthful.
Adopt a kind of gas field of the utility model carbon dioxide to prepare industrial liquid carbon dioxide separation purification system preparedIndustrial liquid carbon dioxide through the Taizhou City product quality supervision and testing institute inspection of national fine chemicals Quality Supervision and Inspection CenterCls analysis, detects 4, sample, testing result altogether:
Data: carbon dioxide content (volume fraction): 99.93%,
Oil content: be up to the standards,
Carbon monoxide, hydrogen sulfide hydrogen phosphide and organic reducing thing: be up to the standards,
Smell: free from extraneous odour,
Moisture dew point :-68 DEG C (4.635ppm)
Check conclusion: after testing, institute's inspection project meets the requirement that GB/T6052-2011 standard specifies to sample.
In sum, the utility model mainly adopts unstripped gas crude separation, distillation, condensation liquefaction, absorption regeneration, high pressure to carryHeat up in a steamer, store supercharging purification technique, integrate absorption method, low temperature processing and high pressure and put forward the technology of heating up in a steamer. This system structure design, companyConnect, rationally distributed, cost is low, makes full use of the native system energy, energy-saving and cost-reducing, realizes gas field carbon dioxide and prepares industrial liquid twoCarbonoxide large-scale production. Prepared industrial liquid carbon dioxide purity, higher than 99.9%, meets state-set standard and industry markStandard, can be widely used in the fields such as welding, chemical industry, the oil field displacement of reservoir oil and engineering science and technology.
Claims (8)
1. gas field carbon dioxide is prepared an industrial liquid carbon dioxide separation purification system, it is characterized in that, mainly by well headSeparative element (1), reboiled distillation unit (2), condensation liquefaction unit (3), absorption regeneration unit (4), high pressure carry heat up in a steamer unit (5) andStore compress cell (6) composition, the gas liquid outlet of described well head separative element (1) and the gas-liquid inlet tube that distills reboiler (21)Line connects, the gaseous phase outlet of distillation reboiler (21) and the middle and lower part gas phase entrance of destilling tower (22), the top of destilling tower (22)The gas phase entrance of gaseous phase outlet and adsorption tower (41), the bottom gaseous phase outlet of adsorption tower (41) and carbon dioxide condenser (51)The liquid-phase outlet of middle part gas phase entrance, carbon dioxide condenser (51) and high pressure are carried the liquid phase entrance that heats up in a steamer tower (52) and are complied with by pipelineInferior head and the tail connect, and high pressure is carried the bottom liquid-phase outlet that heats up in a steamer tower (52) through finished product pans (61) and carbon dioxide storage tank (63) pipelineConnect.
2. a kind of gas field according to claim 1 carbon dioxide is prepared industrial liquid carbon dioxide separation purification system, itsBe characterised in that, described well head separative element (1) is by well head (11), well head separator (12), treatment tank (13) and decompressionValve I (14) composition, in the material outlet of described well head (11) and well head separator (12) entrance, well head separator (12) underPortion's gas liquid outlet is connected by pipeline successively head and the tail with the entrance of pressure-reducing valve I (14), well head separator (12) bottom outlet of sewerBe connected with treatment tank (13) pipeline.
3. a kind of gas field according to claim 1 carbon dioxide is prepared industrial liquid carbon dioxide separation purification system, itsBe characterised in that, described reboiled distillation unit (2) is by distillation reboiler (21), ammonia helical-lobe compressor (212), and destilling tower (22),Carbon dioxide carburettors (23), reflux pump (24) and oil water separator (25) composition, described distillation reboiler (21) respectively withThe gas liquid outlet of pressure-reducing valve I (14), ammonia helical-lobe compressor (212) output, the middle and lower part gas phase entrance of destilling tower (22), distillationThe liquid phase suction line at the outlet of tower (22) bottom liquid phases carbon dioxide and carbon dioxide carburettors (23) middle part connects, described dioxyChanging carbon vaporizer (23) also exports and regeneration gas heat exchanger (42) with oil water separator (25) entrance, outlet surge tank (67) respectivelySuction line connects.
4. a kind of gas field according to claim 1 carbon dioxide is prepared industrial liquid carbon dioxide separation purification system, itsBe characterised in that, described condensation liquefaction unit (3) is made up of phegma condenser (31), phegma pans (32), distillationTower (22) top wherein road gaseous phase outlet phegma is connected with phegma condenser (31) entrance, phegma condenser (31)Liquid-phase outlet is connected with phegma pans (32), reflux pump (24) and destilling tower (22) upper entrance head and the tail pipeline successively.
5. a kind of gas field according to claim 1 carbon dioxide is prepared industrial liquid carbon dioxide separation purification system, itsBe characterised in that, described absorption regeneration unit (4) is by adsorption tower (41), regeneration gas heat exchanger (42), regeneration gas heater (421)And conduction oil cooler (47) composition, described regeneration gas heat exchanger (42) gaseous phase outlet and regeneration gas heater (421) upper endGas phase entrance connects, and regeneration gas heater (421) upper end gaseous phase outlet is connected with the lower bottom of adsorption tower (41), adsorption tower (41) topThe gaseous phase outlet of portion is connected with conduction oil cooler (47) following side.
6. a kind of gas field according to claim 1 carbon dioxide is prepared industrial liquid carbon dioxide separation purification system, itsBe characterised in that, described high pressure is carried and is heated up in a steamer unit (5) and comprise that carbon dioxide condenser (51), high pressure are carried and heat up in a steamer tower (52) and carry and heat up in a steamer tower and boilDevice (53), the liquid-phase outlet of described carbon dioxide condenser (51) and high pressure are carried the liquid phase suction line company of heating up in a steamer tower (52) middle partConnect, high pressure is carried the bottom side liquid-phase outlet that heats up in a steamer tower (52) through finished product pans (61) and pressure-reducing valve II (62) and carbon dioxide storage tank(63) pipeline connects, and carries heating up in a steamer the bottom inlet of tower reboiler (53) and high pressure and carrying and heat up in a steamer tower (52) outlet at bottom, carry and heat up in a steamer tower reboiler(53) top exit and high pressure carry heat up in a steamer tower (52) middle and lower part entrance, carry heat up in a steamer tower reboiler (53) entry and exit, middle part respectivelyBe connected with adsorption tower (41) entrance and regeneration gas heat exchanger (42) outlet line.
7. a kind of gas field according to claim 1 carbon dioxide is prepared industrial liquid carbon dioxide separation purification system, itsBe characterised in that, described storage compress cell (6) comprises carbon dioxide storage tank (63), suction port of compressor heat exchanger (64) and titanium dioxideCarbon compressor (66), the gaseous phase outlet of described carbon dioxide storage tank (63) delays through compressor entrance heat exchanger (64), entrance successivelyRush tank (65), carbon-dioxide gas compressor (66), outlet surge tank (67), carbon dioxide carburettors (23) and regeneration gas heat exchanger(42) pipeline connects.
8. a kind of gas field according to claim 5 carbon dioxide is prepared industrial liquid carbon dioxide separation purification system, itsBe characterised in that, described adsorption tower (41) is set to one and opens one for Double-Tower Structure, and destilling tower (22) is by gate valve I (43) and gate valve II(44) be connected respectively adsorption tower I (411) and adsorption tower II (412) with adsorption tower I (411) and adsorption tower II (412) top entranceLower bottom after gate valve III (45) is connected in parallel with gate valve IV (46), be connected with carbon dioxide condenser (51) entrance.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521055976.5U CN205258018U (en) | 2015-12-17 | 2015-12-17 | Gas field carbon dioxide preparation industry liquid carbon dioxide separation and purification system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521055976.5U CN205258018U (en) | 2015-12-17 | 2015-12-17 | Gas field carbon dioxide preparation industry liquid carbon dioxide separation and purification system |
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| CN205258018U true CN205258018U (en) | 2016-05-25 |
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|---|---|---|---|
| CN201521055976.5U Withdrawn - After Issue CN205258018U (en) | 2015-12-17 | 2015-12-17 | Gas field carbon dioxide preparation industry liquid carbon dioxide separation and purification system |
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| CN (1) | CN205258018U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105502394A (en) * | 2015-12-17 | 2016-04-20 | 江苏华扬液碳有限责任公司 | Separation and purification system for preparing industrial liquid carbon dioxide from gas field carbon dioxide |
| CN111717915A (en) * | 2019-03-19 | 2020-09-29 | 中石化石油工程技术服务有限公司 | Method and device capable of improving capture rate of carbon dioxide in carbon dioxide flooding produced gas of oil field |
-
2015
- 2015-12-17 CN CN201521055976.5U patent/CN205258018U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105502394A (en) * | 2015-12-17 | 2016-04-20 | 江苏华扬液碳有限责任公司 | Separation and purification system for preparing industrial liquid carbon dioxide from gas field carbon dioxide |
| CN111717915A (en) * | 2019-03-19 | 2020-09-29 | 中石化石油工程技术服务有限公司 | Method and device capable of improving capture rate of carbon dioxide in carbon dioxide flooding produced gas of oil field |
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