CN103712414A - Natural gas liquefaction device and liquefaction process of natural gas liquefaction device - Google Patents
Natural gas liquefaction device and liquefaction process of natural gas liquefaction device Download PDFInfo
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Abstract
The invention discloses a natural gas liquefaction device which comprises a feed gas pipe network, a flash steam medium-pressure pipe network, a metering pressure-regulating system, a pre-processing system, a liquefaction system, a heat transfer oil unit, a high-position spreading system and a control system. The metering pressure-regulating system, the pre-processing system and the liquefaction system are mutually communicated through pipes, the metering pressure-regulating system comprises a filter separator and a metering pressure-regulating device, and an accident chain stop valve is arranged in the metering pressure-regulating device. The pre-processing system comprises a CO2 removal unit, a dehydration and debenzolization unit and a desulfuration and demercuration unit. By means of the mode, according to the natural gas liquefaction device, pre-stage pre-processing can be respectively carried out on a refrigeration flow path and a liquidation flow path to remove detrimental impurities in natural gas, and the device safety operation reliability can be improved; CO2 in the natural gas in the refrigeration flow path is not removed, consumption is reduced, the single-set scale of the dehydration, debenzolization and decarbonization processing capacity of the natural gas is large, and the design pressure of low-temperature devices such as plate-fin heat exchangers and booster expansion turbines is high.
Description
Technical field
The present invention relates to natural gas liquefaction device field, particularly relate to a kind of natural gas liquefaction device and liquefaction process thereof.
Background technology
Natural gas is a kind of multi-component mist, and main component is alkane, and wherein methane accounts for the overwhelming majority, separately there are a small amount of ethane, propane and butane, in addition generally also contain hydrogen sulfide, carbon dioxide, nitrogen and aqueous vapor, and the inert gas of trace, as helium and argon etc.Under the status of criterion, methane to butane exists with gaseous state, and pentane is liquid above.Liquefied natural gas (Liquefied Natural Gas is called for short LNG) technology mainly comprises natural gas pretreatment, liquefaction, storage, transports, utilizes five systems.General production process is: natural gas, after purified treatment, adopts throttling, expansion or refrigerant circulation refrigeration process, makes methane become liquid.Natural gas after liquefaction has following features: LNG volume is about with 1/600 of amount gaseous natural gas volume, greatly convenient storage and transportation; LNG efficiency of storage is high, take up an area less, reduced investment; Be conducive to the adjusting of city load, the cold that production process discharges can utilize; LNG is as motor vehicle fuel economy, safety, environmental protection; Produce, use safer; Be conducive to protection of the environment, reduce and pollute.
Natural gas is the most clean fuel of generally acknowledging, generates carbon dioxide and water after combustion of natural gas, with coal and heavy oil comparison, the harmful substance that gas-firing produces significantly reduces, as coal-fired in replaced with natural gas, can reduce nitrogen oxide emission 80-90%, CO emission can reduce 52%.Liquefied natural gas makes natural gas further be purified in liquefaction process, and methane purity is higher, not carbonated, sulfide etc.; and stop the discharge of sulfur dioxide and the generation of Urban Acid Rain; more be conducive to protection of the environment, reduce and pollute, belong to the new industry that state key is helped.
Summary of the invention
The technical problem that the present invention mainly solves is to provide a kind of natural gas liquefaction device and liquefaction process thereof, and gas dehydration takes off benzene, carbonization treatment amount list cover scale is largest domestic, has filled up current domestic blank on atm number processing and liquefaction technology; The Cryo Equipment design pressures such as the plate-fin heat exchanger in equipment, booster expansion turbine are domestic the highest, have filled up current domestic liquefied natural gas in the technical blank of high pressure design and manufacture.
For solving the problems of the technologies described above, the technical scheme that the present invention adopts is: a kind of natural gas liquefaction device is provided, comprise: pressure pipe net, metering voltage-regulating system, pretreatment system, liquefaction system, conduction oil unit, high-order diffusion system and control system in unstripped gas pipe network, flash steam, be interconnected by pipeline between described metering voltage-regulating system, pretreatment system and liquefaction system; Described metering voltage-regulating system comprises filter separator and metering regulator, in metering regulator, is provided with the chain stop valve of accident; Described pretreatment system comprises de-CO
2unit, the de-benzene unit of dehydration and desulfuration demercuration unit, the de-benzene of described dehydration unit is divided into the de-benzene unit of liquefied gas dehydration and the de-benzene of expansion qi exhaustion water unit, and described desulfuration demercuration unit is divided into desulfuration of liquefied gas demercuration unit and expansion desulfurization demercuration unit; Described filter separator access unstripped gas pipe network, and filter separator rear end is connected with described metering regulator, measures after regulator and is connected with respectively and takes off CO
2the de-benzene of unit and expansion qi exhaustion water unit, de-CO
2behind unit, be connected with the de-benzene unit of liquefied gas dehydration and desulfuration of liquefied gas demercuration unit in turn; The de-benzene of described expansion qi exhaustion water is connected with expansion desulfurization demercuration unit behind unit, and described desulfuration of liquefied gas demercuration unit is all connected with described liquefaction system with expansion desulfurization demercuration unit; On described liquefaction system, be connected with ice chest flash steam compressibility and liquefied natural gas storage and handling system, in described liquefied natural gas storage and handling system, be connected with and store flash steam compressibility, store flash steam compressibility and be connected with pressure pipe net in described flash steam.
Preferably, described de-CO
2system comprises CO
2absorption tower, decarbonization gas cooler, decarbonization gas separator, regenerator, poor rich liquid heat exchanger, regeneration gas cooler and regeneration gas separator, CO
2absorption tower is provided with air inlet, gas outlet, inlet and liquid outlet, has inlet, liquid outlet and gas outlet on regenerator; Described CO
2the air inlet on absorption tower is connected with described metering regulator, CO
2the gas outlet on absorption tower is connected with decarbonization gas cooler and decarbonization gas separator in turn, and decarbonization gas separator is connected with the de-benzene of described liquefied gas dehydration unit, CO
2the liquid outlet on absorption tower is connected with flash tank, and flash tank is connected with the inlet of described regenerator; The liquid outlet of described regenerator is connected with poor rich liquid heat exchanger, is connected with lean solution cooler on poor rich liquid heat exchanger, lean solution cooler and described CO
2the inlet on absorption tower is communicated with, lean solution cooler and CO
2pipeline between absorption tower is provided with lean pump and solution strainer, the gas outlet of described regenerator is connected with described regeneration gas cooler, described regeneration gas separator is connected with regeneration gas cooler, on regeneration gas separator, be connected with purifying column and recovery pump, recovery pump is connected with the import of described flash tank; On described regenerator, be connected with reboiler, reboiler is connected with described conduction oil unit.
Preferably, described liquefaction system comprises ice chest and be located at main heat exchanger, subcooler, knockout drum and the decompressor in ice chest, and described ice chest is provided with the supercharger with described decompressor Driven by Coaxial outward; Described main heat exchanger is provided with liquefied gas inlet, flash steam outlet, the import of expansion gas and the outlet of expansion gas, described liquefied gas inlet is connected with described desulfuration of liquefied gas demercuration unit, described flash steam outlet is connected with described ice chest flash steam compressibility, the import of described expansion gas is connected with described expansion desulfurization demercuration unit, described expansion gas outlet is connected with supercharger, pressure pipe net in described flash steam is accessed in supercharger rear end, pipeline in supercharger and flash steam between pressure pipe net is provided with water cooler; Described subcooler is connected with described main heat exchanger with decompressor, and described knockout drum two ends connect respectively subcooler and liquefied natural gas storage and handling system.
Preferably, the de-benzene of described dehydration unit comprises three adsorption towers, and adsorbent is housed in adsorption tower.
Preferably, described desulfuration demercuration unit comprises two desulfuration demercuration towers, and mercury removal agent and desulfurizing agent are housed in desulfuration demercuration tower.
Preferably, described high-order diffusion system comprises spark arrester, knockout drum and high-order exhaust stack, and described spark arrester, knockout drum and high-order exhaust stack are located on the pipeline between pressure pipe net in described unstripped gas pipe network, flash steam, metering voltage-regulating system, pretreatment system, liquefaction system.
Preferably, described control system comprises control centre, clean unit control station, liquefaction unit control station, emergency shutdown system and internal heat system; In described clean unit control station, liquefaction unit control station, emergency shutdown system and internal heat system, be equipped with in-line analyzer and control valve, described clean unit control station, liquefaction unit control station, emergency shutdown system and internal heat system are connected with described control centre by network.
Preferably, described conduction oil unit comprises burner and heat pipe, and burner is connected with described storage flash steam compressibility, and heat pipe is located at described de-CO
2in unit, the de-benzene unit of liquefied gas dehydration and the de-benzene of expansion qi exhaustion water unit.
Preferably, the de-benzene of described liquefied gas dehydration unit, the de-benzene unit of expansion qi exhaustion water and ice chest flash steam compressibility access pressure pipe net in described flash steam, on the pipeline in the de-benzene of liquefied gas dehydration unit, the de-benzene unit of expansion qi exhaustion water and flash steam between pressure pipe net, are equipped with water cooler.
Adopt the natural gas liquefaction process of above-mentioned a kind of natural gas liquefaction device, comprise: high pressure feedstock natural gas is the primary filter through filter separator from unstripped gas pipe network, by metering regulator, raw natural gas is stabilized within the scope of certain pressure again, then measuring regulator is divided into liquefaction stream and swell refrigeration stream by raw natural gas and after imurity-removal, enters ice chest respectively, adopt that natural gas differential pressure expands, throttling refrigeration technique carries out natural gas to obtain after condensation step by step, evaporation, throttling, expansion the refrigerating capacity of different temperatures level, carries out partial liquefaction; Described liquefaction stream adopts N methyldiethanol amine absorption process to remove the carbon dioxide in unstripped gas, absorption method removes water, benzene, sulphur, mercury, then enter main heat exchanger liquefaction in ice chest, the throttling of high-pressure liquefaction natural gas via enters knockout drum, and the product liquefied natural gas after liquefaction system liquefaction is sent into storage tank; The flash steam low-pressure tail gas of flash distillation is cooling box after master changes re-heat, then conduct takes off CO after compressor supercharging
2the cold blowing regeneration gas of unit, regeneration gas is returned middle pressure pipe net after water cooling; The Gas Exploitation of described expansion stream removes water, heavy hydrocarbon and mercury by absorption method; Then enter ice chest expands and produces the required part cold of liquefaction, the natural gas via main heat exchanger re-heat cooling box after expansion through decompressor again after main heat exchanger is cooling; After the supercharger supercharging coaxially dragging via decompressor again, as regeneration heating gas, after regeneration gas is cooling, compress rear gas with flash steam and converge.
The invention has the beneficial effects as follows: the present invention's stream that freezes carries out respectively prime pretreatment and removes the objectionable impurities in natural gas with liquefaction stream, improves equipment safety operation reliability; Refrigeration stream natural gas does not remove CO
2, reduce and consume.
Accompanying drawing explanation
Fig. 1 is the structural representation of a kind of natural gas liquefaction device of the present invention;
Fig. 2 is de-CO in described a kind of natural gas liquefaction device
2the structural representation of unit;
In accompanying drawing, the mark of each parts is as follows: 1, unstripped gas pipe network; 2, pressure pipe net in flash steam; 3, filter separator; 4, metering regulator; 5, de-CO
2unit; 6, the de-benzene of expansion qi exhaustion water unit; 7, the de-benzene of liquefied gas dehydration unit; 8, desulfuration of liquefied gas demercuration unit; 9, expansion desulfurization demercuration unit; 10, liquefaction system; 11, conduction oil unit; 12, ice chest flash steam compressibility; 13, liquefied natural gas storage and handling system; 14, store flash steam compressibility; 15, water cooler; 51, CO
2absorption tower; 52, decarbonization gas cooler; 53, decarbonization gas separator; 54, regenerator; 55, poor rich liquid heat exchanger; 56, regeneration gas cooler; 57, regeneration gas separator; 58, flash tank; 59, solution strainer; 510, recovery pump; 511, reboiler.
The specific embodiment
Below in conjunction with accompanying drawing, preferred embodiment of the present invention is described in detail, thereby so that advantages and features of the invention can be easier to be it will be appreciated by those skilled in the art that, protection scope of the present invention is made to more explicit defining.
Refer to Fig. 1 and Fig. 2, the embodiment of the present invention comprises:
A kind of natural gas liquefaction device, comprise: pressure pipe net 2, metering voltage-regulating system, pretreatment system, liquefaction system 10, conduction oil unit 11, high-order diffusion system and control system in unstripped gas pipe network 1, flash steam, be interconnected by pipeline between described metering voltage-regulating system, pretreatment system and liquefaction system 10; Described metering voltage-regulating system comprises filter separator 3 and metering regulator 4, in metering regulator 4, is provided with the chain stop valve of accident; Described pretreatment system comprises de-CO
2unit 5, the de-benzene unit of dehydration and desulfuration demercuration unit; The de-benzene of described dehydration unit comprises three adsorption towers, adsorbent is housed in adsorption tower, the de-benzene of dehydration unit adopts three-column process flow, utilize adsorbent adsorption capacity at different pressures and temperature to there are differences and select the characteristic of absorption, remove the heavy hydrocarbons impurity in gas, three adsorption tower continuous circulations are used, an adsorption tower job, another two adsorption towers are the different phase in adsorbent reactivation, in adsorption tower, benzene ring compound is removed to and is less than or equal to 10ppm, and other hydro carbons is removed to and meets the demands; The de-benzene of dehydration unit is divided into the de-benzene unit 7 of liquefied gas dehydration and the de-benzene of expansion qi exhaustion water unit 6; The natural gas coming from prime unit enters desulfuration demercuration tower, the in-built mercury removal agent of tower and desulfurizing agent, sulphur on mercury and desulfurizing agent (soaking sulphur active carbon) produces chemical reaction and generates mercuric sulphide, be adsorbed on active carbon, thereby reach the object that removes mercury, from the mercury content of system natural gas out, be less than 0.01 μ g/Nm
3.Sulfide is less than 3.5mg/Nm
3(4ppmV), desulfuration demercuration unit is divided into desulfuration of liquefied gas demercuration unit 8 and expansion desulfurization demercuration unit 9; Described filter separator 3 access unstripped gas pipe networks, and filter separator 3 rear ends are connected with described metering regulator 4, measure rear being connected with respectively of regulator 4 and take off CO
2the de-benzene of unit 5 and expansion qi exhaustion water unit 6, de-CO
2behind unit 5, be connected with the de-benzene unit 7 of liquefied gas dehydration and desulfuration of liquefied gas demercuration unit 8 in turn; Behind the de-benzene of described expansion qi exhaustion water unit 6, be connected with expansion desulfurization demercuration unit 9, described desulfuration of liquefied gas demercuration unit 8 is all connected with described liquefaction system 10 with expansion desulfurization demercuration unit 9; On described liquefaction system 10, be connected with ice chest flash steam compressibility 12 and liquefied natural gas storage and handling system 13, in described liquefied natural gas storage and handling system 13, be connected with and store flash steam compressibility 14, store flash steam compressibility 14 and be connected with pressure pipe net 2 in described flash steam.Described conduction oil unit 11 comprises burner and heat pipe, and burner is connected with described storage flash steam compressibility 14, and heat pipe is located at described de-CO
2in unit 5, the de-benzene unit 7 of liquefied gas dehydration and the de-benzene of expansion qi exhaustion water unit 6; The de-benzene of described liquefied gas dehydration unit 7, the de-benzene unit 6 of expansion qi exhaustion water and the compression of ice chest flash steam are pressure pipe net 2 in the described flash steam of 12 access, on the pipeline in the de-benzene of liquefied gas dehydration unit 7, the de-benzene unit 6 of expansion qi exhaustion water and flash steam between pressure pipe net 2, are equipped with water cooler 15.
Described de-CO
2unit 5 comprises CO
2absorption tower 51, decarbonization gas cooler 52, decarbonization gas separator 53, regenerator 54, poor rich liquid heat exchanger 55, regeneration gas cooler 56 and regeneration gas separator 57, CO
2absorption tower 51 is provided with air inlet, gas outlet, inlet and liquid outlet, has inlet, liquid outlet and gas outlet on regenerator 54; Described CO
2the air inlet on absorption tower 51 is connected with described metering regulator 4, CO
2the gas outlet on absorption tower 51 is connected with decarbonization gas cooler 52 and decarbonization gas separator 53 in turn, and decarbonization gas separator 53 is connected with the de-benzene of described liquefied gas dehydration unit 7, CO
2the liquid outlet on absorption tower 51 is connected with flash tank 58, and flash tank 58 is connected with the inlet of described regenerator 54; The liquid outlet of described regenerator 54 is connected with poor rich liquid heat exchanger 55, is connected with lean solution cooler on poor rich liquid heat exchanger 55, lean solution cooler and described CO
2the inlet on absorption tower 51 is communicated with, lean solution cooler and CO
2pipeline between absorption tower is provided with lean pump and solution strainer 59, the gas outlet of described regenerator 54 is connected with described regeneration gas cooler 56, described regeneration gas separator 57 is connected with regeneration gas cooler 56, on regeneration gas separator 57, be connected with purifying column and recovery pump 510, recovery pump 510 is connected with the import of described flash tank 58; On described regenerator 54, be connected with reboiler 511, reboiler 511 is connected with described conduction oil unit 11.Natural gas is from CO
251 bottoms, absorption tower enter, and pass through CO from bottom to top
2absorption tower 51, amine aqueous solution (lean solution) is from CO
251 tops, absorption tower enter, and pass through CO from top to bottom
2absorption tower 51, the amine aqueous solution of reverse flow and natural gas are at CO
2the interior abundant contact in absorption tower 51, the CO in gas
2be absorbed and enter liquid phase, unabsorbed component is from CO
2absorption tower 51 Base top contacts, enter decarbonization gas cooler 52, cool the temperature to≤40 ℃, enter decarbonization gas separator 53, then enter subsequent technique; Absorb CO
2amine aqueous solution claim rich solution, after solution (lean solution) heat exchange of flowing out with regenerator 54 bottoms, to regenerator 54 tops, at regenerator 54, carry out steam stripping regeneration, until the lean solution degree of lean solution touches the mark, the lean solution that goes out regenerator 54 is passed through poor rich liquid heat exchanger 55, is entered lean solution cooler, and through lean pump pressurization, temperature enters CO in the time of 45～65 ℃
251 tops, absorption tower; Regenerator 54 top exit gases, through regeneration gas cooler 56, enter regeneration gas separator 57, go out gas emptying or concentrated discharge after purification utensil of separator, and condensate liquid removes underground tank.
Described liquefaction system 10 comprises ice chest and be located at main heat exchanger, subcooler, knockout drum and the decompressor in ice chest, and described main heat exchanger is Long plate type heat exchanger, and described ice chest is provided with the supercharger with described decompressor Driven by Coaxial outward; Described main heat exchanger is provided with liquefied gas inlet, flash steam outlet, the import of expansion gas and the outlet of expansion gas, described liquefied gas inlet is connected with described desulfuration of liquefied gas demercuration unit 8, described flash steam outlet is connected with described ice chest flash steam compressibility 12, the import of described expansion gas is connected with described expansion desulfurization demercuration unit 9, described expansion gas outlet is connected with supercharger, pressure pipe net 2 in described flash steam is accessed in supercharger rear end, pipeline in supercharger and flash steam between pressure pipe net 2 is provided with water cooler 15; Described subcooler is connected with described main heat exchanger with decompressor, and described knockout drum two ends connect respectively subcooler and liquefied natural gas storage and handling system 13.
Described high-order diffusion system comprises spark arrester, knockout drum and high-order exhaust stack, described spark arrester, knockout drum and high-order exhaust stack are located on the pipeline between pressure pipe net 2 in described unstripped gas pipe network 1, flash steam, metering voltage-regulating system, pretreatment system, liquefaction system 10, the security reliability of assurance device and whole equipment battery limit (BL).
Described control system comprises control centre, clean unit control station, liquefaction unit control station, emergency shutdown system and internal heat system; In described clean unit control station, liquefaction unit control station, emergency shutdown system and internal heat system, be equipped with in-line analyzer and control valve; described clean unit control station, liquefaction unit control station, emergency shutdown system and internal heat system are connected with described control centre by network; except guaranteeing the normal operation of equipment; safeguard measure can also when appearring in equipment, disastershutdown be provided; the position of the abort situation of all by-pass valve controls in a safety, guarantees device security.
A kind of natural gas liquefaction process, high pressure feedstock natural gas is the primary filter through filter separator 3 from unstripped gas pipe network 1, by metering regulator 4, raw natural gas is stabilized within the scope of certain pressure again, then be divided into liquefaction stream and swell refrigeration stream, liquefaction stream adopts N methyldiethanol amine absorption process to remove the carbon dioxide in unstripped gas, absorption method removes water, benzene, sulphur, mercury, then enter main heat exchanger liquefaction in ice chest, high pressure LNG enters knockout drum through throttling, and the product LNG after liquefaction system liquefaction sends into storage tank; The BOG low-pressure tail gas of flash distillation is cooling box after master changes re-heat, then conduct takes off CO after compressor supercharging
2the cold blowing regeneration gas of unit, regeneration gas is returned middle pressure pipe net after water cooling; The Gas Exploitation of expansion stream removes water, heavy hydrocarbon and mercury by absorption method; Then enter liquefaction ice chest expands and produces the required part cold of liquefaction, the natural gas via main heat exchanger re-heat cooling box after expansion through decompressor again after main heat exchanger is cooling; After the supercharger supercharging coaxially dragging via decompressor again, as regeneration heating gas, after regeneration gas is cooling, compress rear gas with BOG and converge.
A kind of natural gas liquefaction device of the present invention, natural gas processing amount 5,000,000 Nm
3/ h, unit scale is maximum at home at present; Raw natural gas pressure 8.0MPa, the Cryo Equipment design pressures such as plate-fin heat exchanger, booster expansion turbine at present at home in liquefied natural gas plant for the highest; According to technological process tissue and requirement, refrigeration stream carries out respectively prime pretreatment with liquefaction stream and removes the objectionable impurities in natural gas, improves equipment safety operation reliability; Refrigeration stream natural gas does not remove CO
2, reduce and consume.
The foregoing is only embodiments of the invention; not thereby limit the scope of the claims of the present invention; every equivalent structure or conversion of equivalent flow process that utilizes description of the present invention and accompanying drawing content to do; or be directly or indirectly used in other relevant technical fields, be all in like manner included in scope of patent protection of the present invention.
Claims (10)
1. a natural gas liquefaction device, it is characterized in that, comprise: pressure pipe net, metering voltage-regulating system, pretreatment system, liquefaction system, conduction oil unit, high-order diffusion system and control system in unstripped gas pipe network, flash steam, be interconnected by pipeline between described metering voltage-regulating system, pretreatment system and liquefaction system; Described metering voltage-regulating system comprises filter separator and metering regulator, in metering regulator, is provided with the chain stop valve of accident; Described pretreatment system comprises de-CO
2unit, the de-benzene unit of dehydration and desulfuration demercuration unit, the de-benzene of described dehydration unit is divided into the de-benzene unit of liquefied gas dehydration and the de-benzene of expansion qi exhaustion water unit, and described desulfuration demercuration unit is divided into desulfuration of liquefied gas demercuration unit and expansion desulfurization demercuration unit; Described filter separator access unstripped gas pipe network, and filter separator rear end is connected with described metering regulator, measures after regulator and is connected with respectively and takes off CO
2the de-benzene of unit and expansion qi exhaustion water unit, de-CO
2behind unit, be connected with the de-benzene unit of liquefied gas dehydration and desulfuration of liquefied gas demercuration unit in turn; The de-benzene of described expansion qi exhaustion water is connected with expansion desulfurization demercuration unit behind unit, and described desulfuration of liquefied gas demercuration unit is all connected with described liquefaction system with expansion desulfurization demercuration unit; On described liquefaction system, be connected with ice chest flash steam compressibility and liquefied natural gas storage and handling system, in described liquefied natural gas storage and handling system, be connected with and store flash steam compressibility, store flash steam compressibility and be connected with pressure pipe net in described flash steam.
2. a kind of natural gas liquefaction device according to claim 1, is characterized in that: described de-CO
2system comprises CO
2absorption tower, decarbonization gas cooler, decarbonization gas separator, regenerator, poor rich liquid heat exchanger, regeneration gas cooler and regeneration gas separator, CO
2absorption tower is provided with air inlet, gas outlet, inlet and liquid outlet, has inlet, liquid outlet and gas outlet on regenerator; Described CO
2the air inlet on absorption tower is connected with described metering regulator, CO
2the gas outlet on absorption tower is connected with decarbonization gas cooler and decarbonization gas separator in turn, and decarbonization gas separator is connected with the de-benzene of described liquefied gas dehydration unit, CO
2the liquid outlet on absorption tower is connected with flash tank, and flash tank is connected with the inlet of described regenerator; The liquid outlet of described regenerator is connected with poor rich liquid heat exchanger, is connected with lean solution cooler on poor rich liquid heat exchanger, lean solution cooler and described CO
2the inlet on absorption tower is communicated with, lean solution cooler and CO
2pipeline between absorption tower is provided with lean pump and solution strainer, the gas outlet of described regenerator is connected with described regeneration gas cooler, described regeneration gas separator is connected with regeneration gas cooler, on regeneration gas separator, be connected with purifying column and recovery pump, recovery pump is connected with the import of described flash tank; On described regenerator, be connected with reboiler, reboiler is connected with described conduction oil unit.
3. a kind of natural gas liquefaction device according to claim 1, it is characterized in that: described liquefaction system comprises ice chest and be located at main heat exchanger, subcooler, knockout drum and the decompressor in ice chest, and described ice chest is provided with the supercharger with described decompressor Driven by Coaxial outward; Described main heat exchanger is provided with liquefied gas inlet, flash steam outlet, the import of expansion gas and the outlet of expansion gas, described liquefied gas inlet is connected with described desulfuration of liquefied gas demercuration unit, described flash steam outlet is connected with described ice chest flash steam compressibility, the import of described expansion gas is connected with described expansion desulfurization demercuration unit, described expansion gas outlet is connected with supercharger, pressure pipe net in described flash steam is accessed in supercharger rear end, pipeline in supercharger and flash steam between pressure pipe net is provided with water cooler; Described subcooler is connected with described main heat exchanger with decompressor, and described knockout drum two ends connect respectively subcooler and liquefied natural gas storage and handling system.
4. a kind of natural gas liquefaction device according to claim 1, is characterized in that: the de-benzene of described dehydration unit comprises three adsorption towers, and adsorbent is housed in adsorption tower.
5. a kind of natural gas liquefaction device according to claim 1, is characterized in that: described desulfuration demercuration unit comprises two desulfuration demercuration towers, and mercury removal agent and desulfurizing agent are housed in desulfuration demercuration tower.
6. a kind of natural gas liquefaction device according to claim 1, it is characterized in that: described high-order diffusion system comprises spark arrester, knockout drum and high-order exhaust stack, described spark arrester, knockout drum and high-order exhaust stack are located on the pipeline between pressure pipe net in described unstripped gas pipe network, flash steam, metering voltage-regulating system, pretreatment system, liquefaction system.
7. a kind of natural gas liquefaction device according to claim 1, is characterized in that: described control system comprises control centre, clean unit control station, liquefaction unit control station, emergency shutdown system and internal heat system; In described clean unit control station, liquefaction unit control station, emergency shutdown system and internal heat system, be equipped with in-line analyzer and control valve, described clean unit control station, liquefaction unit control station, emergency shutdown system and internal heat system are connected with described control centre by network.
8. a kind of natural gas liquefaction device according to claim 1, is characterized in that: described conduction oil unit comprises burner and heat pipe, and burner is connected with described storage flash steam compressibility, and heat pipe is located at described de-CO
2in unit, the de-benzene unit of liquefied gas dehydration and the de-benzene of expansion qi exhaustion water unit.
9. a kind of natural gas liquefaction device according to claim 1, it is characterized in that: the de-benzene of described liquefied gas dehydration unit, the de-benzene unit of expansion qi exhaustion water and ice chest flash steam compressibility access pressure pipe net in described flash steam, on the pipeline in the de-benzene of liquefied gas dehydration unit, the de-benzene unit of expansion qi exhaustion water and flash steam between pressure pipe net, be equipped with water cooler.
10. adopt the natural gas liquefaction process of a kind of natural gas liquefaction device claimed in claim 1, it is characterized in that, comprise: high pressure feedstock natural gas is the primary filter through filter separator from unstripped gas pipe network, by metering regulator, raw natural gas is stabilized within the scope of certain pressure again, then measuring regulator is divided into liquefaction stream and swell refrigeration stream by raw natural gas and after imurity-removal, enters ice chest respectively, adopt natural gas differential pressure to expand, throttling refrigeration technique is carried out condensation step by step by natural gas, evaporation, throttling, after expansion, obtain the refrigerating capacity of different temperatures level, carry out partial liquefaction, described liquefaction stream adopts N methyldiethanol amine absorption process to remove the carbon dioxide in unstripped gas, absorption method removes water, benzene, sulphur, mercury, then enter main heat exchanger liquefaction in ice chest, the throttling of high-pressure liquefaction natural gas via enters knockout drum, and the product liquefied natural gas after liquefaction system liquefaction is sent into storage tank, the flash steam low-pressure tail gas of flash distillation is cooling box after master changes re-heat, then conduct takes off CO after compressor supercharging
2the cold blowing regeneration gas of unit, regeneration gas is returned middle pressure pipe net after water cooling, the Gas Exploitation of described expansion stream removes water, heavy hydrocarbon and mercury by absorption method, then enter ice chest expands and produces the required part cold of liquefaction, the natural gas via main heat exchanger re-heat cooling box after expansion through decompressor again after main heat exchanger is cooling, after the supercharger supercharging coaxially dragging via decompressor again, as regeneration heating gas, after regeneration gas is cooling, compress rear gas with flash steam and converge.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310751278.8A CN103712414B (en) | 2013-12-31 | 2013-12-31 | A kind of natural gas liquefaction device and its liquefaction process |
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| CN201310751278.8A CN103712414B (en) | 2013-12-31 | 2013-12-31 | A kind of natural gas liquefaction device and its liquefaction process |
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| CN103712414A true CN103712414A (en) | 2014-04-09 |
| CN103712414B CN103712414B (en) | 2018-08-17 |
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| CN103712414B (en) | 2018-08-17 |
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