CN111454758B - An efficient and compact natural gas glycol dehydration system and method - Google Patents
An efficient and compact natural gas glycol dehydration system and method Download PDFInfo
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- CN111454758B CN111454758B CN202010279907.1A CN202010279907A CN111454758B CN 111454758 B CN111454758 B CN 111454758B CN 202010279907 A CN202010279907 A CN 202010279907A CN 111454758 B CN111454758 B CN 111454758B
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- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 title claims abstract description 389
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 258
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 title claims abstract description 175
- 239000003345 natural gas Substances 0.000 title claims abstract description 128
- 230000018044 dehydration Effects 0.000 title claims abstract description 58
- 238000006297 dehydration reaction Methods 0.000 title claims abstract description 58
- 238000000034 method Methods 0.000 title claims abstract description 58
- 239000007788 liquid Substances 0.000 claims abstract description 237
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 212
- ZIBGPFATKBEMQZ-UHFFFAOYSA-N triethylene glycol Chemical compound OCCOCCOCCO ZIBGPFATKBEMQZ-UHFFFAOYSA-N 0.000 claims abstract description 152
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 74
- 239000006096 absorbing agent Substances 0.000 claims abstract description 59
- 238000003860 storage Methods 0.000 claims abstract description 26
- 230000008929 regeneration Effects 0.000 claims abstract description 19
- 238000011069 regeneration method Methods 0.000 claims abstract description 19
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract 2
- 239000007789 gas Substances 0.000 claims description 112
- 239000012071 phase Substances 0.000 claims description 81
- 238000012546 transfer Methods 0.000 claims description 49
- 239000007791 liquid phase Substances 0.000 claims description 44
- 238000002347 injection Methods 0.000 claims description 13
- 239000007924 injection Substances 0.000 claims description 13
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 claims description 12
- 238000000889 atomisation Methods 0.000 claims description 11
- 239000002245 particle Substances 0.000 claims description 11
- 238000000926 separation method Methods 0.000 claims description 10
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 9
- 238000012856 packing Methods 0.000 claims description 9
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 claims description 6
- 238000004581 coalescence Methods 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims description 4
- 239000012535 impurity Substances 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 4
- 238000011084 recovery Methods 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 4
- 239000010865 sewage Substances 0.000 claims description 4
- 239000007787 solid Substances 0.000 claims description 4
- NHTMVDHEPJAVLT-UHFFFAOYSA-N Isooctane Chemical group CC(C)CC(C)(C)C NHTMVDHEPJAVLT-UHFFFAOYSA-N 0.000 claims description 3
- 238000009835 boiling Methods 0.000 claims description 3
- JVSWJIKNEAIKJW-UHFFFAOYSA-N dimethyl-hexane Natural products CCCCCC(C)C JVSWJIKNEAIKJW-UHFFFAOYSA-N 0.000 claims description 3
- 238000012545 processing Methods 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 2
- 239000000126 substance Substances 0.000 claims description 2
- 239000003595 mist Substances 0.000 claims 8
- 238000013508 migration Methods 0.000 claims 1
- 230000005012 migration Effects 0.000 claims 1
- 238000010521 absorption reaction Methods 0.000 abstract description 26
- 230000002745 absorbent Effects 0.000 abstract description 6
- 239000002250 absorbent Substances 0.000 abstract description 6
- 208000005156 Dehydration Diseases 0.000 description 45
- 239000000243 solution Substances 0.000 description 26
- 238000007599 discharging Methods 0.000 description 12
- 238000009434 installation Methods 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 7
- 238000001914 filtration Methods 0.000 description 7
- 238000011161 development Methods 0.000 description 4
- 230000018109 developmental process Effects 0.000 description 4
- 239000006185 dispersion Substances 0.000 description 4
- 230000007547 defect Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000007667 floating Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 230000016507 interphase Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000005501 phase interface Effects 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/106—Removal of contaminants of water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
- B01D3/322—Reboiler specifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/343—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances the substance being a gas
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0027—Condensation of vapours; Recovering volatile solvents by condensation by direct contact between vapours or gases and the cooling medium
- B01D5/003—Condensation of vapours; Recovering volatile solvents by condensation by direct contact between vapours or gases and the cooling medium within column(s)
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
- B01D53/261—Drying gases or vapours by adsorption
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/107—Limiting or prohibiting hydrate formation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/202—Alcohols or their derivatives
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Gas Separation By Absorption (AREA)
Abstract
本发明公开了一种适用于海上平台的高效紧凑型管式天然气甘醇脱水系统及方法，包括过滤分离器底流阀、过滤分离器、管式气液接触吸收器、三甘醇冷凝器、甘醇泵、天然气/贫甘醇换热器、除雾器、除雾器底流阀、贫甘醇储罐、贫/富甘醇换热器、管式气液接触解吸器、冷凝器、三相分离器、汽提剂泵、聚结器、聚结器排水阀、汽提剂干燥器、汽提剂加热器、再沸器、甘醇过滤器、闪蒸罐。天然气三甘醇接触吸收脱水部分采用管式气液接触吸收器，三甘醇再生部分采用管式富甘醇解吸器，能降低设备高度、体积和重量；使用该三甘醇贫液作为吸收剂，可使吸收系统中经吸水处理的天然气出口水露点降低至‑60℃以下；减少三甘醇循环量和损失，大大节省操作运行成本，有效减小海上平台的空间占用，能够满足海上平台等空间受限场合长输和液化用天然气的处理要求。
The invention discloses a high-efficiency and compact tubular natural gas glycol dehydration system and method suitable for offshore platforms, comprising a filter separator underflow valve, a filter separator, a tubular gas-liquid contact absorber, a triethylene glycol condenser, a Alcohol pump, natural gas/lean glycol heat exchanger, demister, demister underflow valve, lean glycol storage tank, lean/rich glycol heat exchanger, tubular gas-liquid contact desorber, condenser, three-phase Separator, stripping agent pump, coalescer, coalescer drain valve, stripping agent dryer, stripping agent heater, reboiler, glycol filter, flash tank. The natural gas triethylene glycol contact absorption and dehydration part adopts a tubular gas-liquid contact absorber, and the triethylene glycol regeneration part adopts a tubular rich glycol desorber, which can reduce the height, volume and weight of the equipment; the triethylene glycol depleted liquid is used as an absorbent , which can reduce the dew point of the natural gas outlet water after water absorption treatment in the absorption system to below ‑60 °C; reduce the amount and loss of triethylene glycol circulation, greatly save operating costs, effectively reduce the space occupation of offshore platforms, and can meet the needs of offshore platforms, etc. Handling requirements for natural gas for long-distance transportation and liquefaction in space-constrained applications.
Description
Technical Field
The invention relates to a natural gas processing technology, in particular to a high-efficiency compact natural gas glycol dehydration system and a method.
Background
With the increasing demand for energy in the current society and the increasing awareness of environmental protection, natural gas is used as clean energy, and more attention is paid to the development and utilization of natural gas. However, with the gradual depletion of onshore oil and gas resources, offshore oil and gas field development will gradually become a strategic take-over hotspot. Although natural gas produced from offshore fields is typically transported by pipeline to onshore terminals for purification, dehydration of the natural gas is often required on the offshore platform prior to export to prevent plugging of the pipeline by hydrate formation and corrosion damage to the pipeline by water binding with acid gases.
At present, the dehydration method of natural gas mainly comprises a supersonic separation method, a freezing separation method, an adsorption method and an absorption method. Considering the operation economy, the triethylene glycol absorption method is generally adopted at present in offshore gas fields at home and abroad, but the method has the defects of complex flow, large volume and weight of a triethylene glycol absorption tower, high energy consumption of a triethylene glycol regeneration system and the like. Specifically, the triethylene glycol absorption tower generally adopts a bubble cap absorption tower, a filler absorption tower, a cyclone tube type absorption tower and the like at present, gas-liquid countercurrent mass transfer is realized mainly by means of gravity, in order to prevent flooding and entrainment, the gas velocity of an empty tower is usually not more than 1.5-2 m/s, and the gas-liquid volume mass transfer coefficient is small, so that tower type absorption equipment has the defects of low mass transfer efficiency, large weight and occupied area and the like, and occupies a large amount of precious deck area and size space of an offshore platform. With the gradual progress of the development of ocean oil and gas towards deep water and ultra-deep water sea areas, a large number of floating platforms have to be adopted, but the requirement of the floating platforms on the upper load is severe, so that the development of an efficient compact natural gas glycol dehydration system and method is urgently needed.
Researchers propose that the absorption mass transfer process is strengthened by adopting a gas-liquid parallel flow mode in a pipe, gas to be purified flows in the pipe at a high speed, liquid absorbent is injected into high-speed gas flow in the pipe, the injected liquid absorbent is torn and broken into tiny liquid filaments and liquid drops by the high-speed gas flow, and the atomized absorbent and the high-speed gas flow are fully mixed in the process of flowing in the same direction in the space in the pipe to absorb mass transfer. After the absorbent is atomized, the gas-liquid contact area is obviously increased, and violent turbulence and a rapidly updated interphase interface are generated in the gas-liquid two-phase parallel flow process, so that the increase of the total volume mass transfer coefficient is facilitated, and the mass transfer process of the gas-liquid two-phase is greatly enhanced. The ExxonMobil upflow Research company in US patent US 8899557 proposes to use a tubular gas-liquid co-current contactor to replace the traditional absorption tower, improves the existing natural gas dehydration and deacidification purification process device, can reduce the weight and volume of the contact absorption equipment, is suitable for the exploitation and purification process of shale gas fields generally in remote areas, and is not sensitive to gravity and shaking, and is also very suitable for offshore platforms. The U.S. patent US20170145803 provides a compact underwater dewatering system and method, a tubular gas-liquid parallel-flow contact absorber is adopted to replace a traditional absorption tower, an atomization component in the tubular gas-liquid parallel-flow contact absorber atomizes a liquid absorbent into micron-sized liquid drops in high-speed gas flow in a tube, the mixed absorption mass transfer process between gas and liquid is strengthened, and the tubular gas-liquid parallel-flow contactor has the advantages of large handling capacity, light weight, small pipe diameter, capability of bearing seabed high pressure and convenience in seabed installation and arrangement. The process and apparatus disclosed in the above patents are considered to be replaced by a compact and efficient tubular gas-liquid co-current contacting absorber in the form of a conventional absorption column, which is bulky and heavy, while the conventional rectification column is still used in the glycol regeneration system to regenerate the glycol. The rectification column is a thin and high tower type mass transfer device, the installation still has requirements on the height, the operation treatment process is easily influenced by the shaking of a platform, the application of the traditional regeneration system on an offshore platform is obviously not compact enough, and the requirements of the rectification column on the height space limit the installation of the rectification column on the deck of the platform.
The invention discloses that the Beijing university of chemical industry in patent CN 107641536 and patent CN 104194854 uses a supergravity machine to replace a traditional absorption tower and a regenerative rectifying column, and uses a rotor rotating at high speed to generate centrifugal force to break liquid into tiny liquid films and liquid drops, so that the phase interface is thinner and faster, the gas-liquid mass transfer process is strengthened, the mass transfer efficiency of a triethylene glycol-natural gas dehydration system is improved, and the size of dehydration equipment is reduced. However, the supergravity machine has the disadvantages that the internal rotor rotates at high speed when in operation, the daily maintenance cost of the internal rotor as a moving device is high, the system reliability is poor, the installation requirement of the device on the support is high especially under the condition of large processing capacity, and the defects limit the application of the internal rotor in the field.
Disclosure of Invention
The invention aims to provide an efficient and compact natural gas glycol dehydration system and method.
The purpose of the invention is realized by the following technical scheme:
the invention relates to a high-efficiency compact natural gas glycol dehydration system, which comprises a filtering separator underflow valve 1, a filtering separator 2, a tubular gas-liquid contact absorber 3, a triethylene glycol condenser 4, a glycol pump 5, a natural gas/lean glycol heat exchanger 6, a demister 7, a demister underflow valve 8, a lean glycol storage tank 9, a lean/rich glycol heat exchanger 10, a tubular gas-liquid contact desorber 11, a condenser 12, a three-phase separator 13, a stripping agent pump 14, a first stop valve 15, a stripping agent injection stop valve 16, a coalescer 17, a coalescer drain valve 18, a first stripping agent dryer 19, a second stripping agent dryer 20, a stripping agent heater 21, a reboiler 22, a glycol filter 23, a flash tank 24 and a second stop valve 25 which are connected through pipelines;
the bottom outlet of the filter separator 2 is connected with a filter separator underflow valve 1, the outlet of the filter separator underflow valve 1 is connected with a downstream sewage disposal system, and the top outlet of the filter separator 2 is connected with a gas phase inlet of a tubular gas-liquid contact absorber 3;
a gas phase outlet of the tubular gas-liquid contact absorber 3 is connected with a natural gas inlet of a natural gas/lean glycol heat exchanger 6, a natural gas outlet of the natural gas/lean glycol heat exchanger 6 is connected with an inlet of a demister 7, a gas phase outlet at the upper part of the demister 7 is connected with a downstream natural gas treatment section, a liquid phase outlet at the lower part of the demister 7 is connected with an inlet of a demister underflow valve 8, and an outlet of the demister underflow valve 8 is connected with a flash tank 24;
a liquid phase outlet at the lower part of the tubular gas-liquid contact absorber 3 is connected with a second stop valve 25, the second stop valve 25 is connected with a flash drum 24, a gas phase outlet at the upper part of the flash drum 24 is connected with a tail gas treatment system, a liquid phase outlet at the bottom of the flash drum 24 is connected with an inlet of a glycol filter 23, an outlet of the glycol filter 23 is connected with a glycol-rich inlet of the lean/glycol-rich heat exchanger 10, a glycol-rich outlet of the lean/glycol-rich heat exchanger 10 is connected with a liquid phase inlet of the tubular gas-liquid contact desorber 11, and a liquid phase outlet of the tubular gas-liquid contact desorber 11 is connected with an inlet at the upper part of the reboiler 22;
a gas phase outlet of the tubular gas-liquid contact desorber 11 is connected with an inlet of a condenser 12, an outlet of the condenser 12 is connected with an inlet of a three-phase separator 13, a non-condensable gas outlet of the three-phase separator 13 leads to tail gas treatment, and a water outlet is arranged at the lower end of the three-phase separator 13;
the outlet of the stripping agent of the three-phase separator 13 is connected with the inlet of a stripping agent pump 14, the outlet of the stripping agent pump 14 is connected with the inlet of a stripping agent coalescer 17, the outlet of the stripping agent coalescer 17 is connected with the inlet of a first stripping agent dryer 19, the upper part of the stripping agent coalescer 17 is provided with a stripping agent feeding port and is connected with a stripping agent injection stop valve 16, the stripping agent is fed through the inlet of the stripping agent injection stop valve 16, and the lower part of the stripping agent coalescer 17 is provided with a water drain port and is connected with a coalescer drain valve 18;
the first stripping agent dryer 19, the second stripping agent dryer 20 and the stripping agent heater 21 are sequentially connected, and an outlet of the stripping agent heater 21 is connected with a stripping agent inlet at the lower part of the reboiler 22 to realize circulation of the stripping agent;
the gas phase outlet of the reboiler 22 is connected with the gas phase inlet of the tubular gas-liquid contact desorber 11, the liquid phase outlet of the reboiler 22 is connected with the lean glycol inlet of the lean/rich glycol heat exchanger 6, the lean glycol outlet of the lean/rich glycol heat exchanger 6 is connected with the inlet of the lean glycol storage tank 9, the bottom outlet of the lean glycol storage tank 9 is connected with the lean glycol inlet of the natural gas/lean glycol heat exchanger 6, the lean glycol outlet of the natural gas/lean glycol heat exchanger 9 is connected with the inlet of the glycol pump 5, the outlet of the glycol pump 5 is connected with the inlet of the triethylene glycol condenser 4, and the outlet of the triethylene glycol condenser 4 is connected with the liquid phase inlet of the tubular gas-liquid contact absorber 3, so that the circulation of the triethylene glycol is realized.
The tubular gas-liquid contact absorber is characterized in that the atomizing part is a tubular atomizer or a wire mesh packing, and the gas-liquid separation part is a demisting tubular gas-liquid separator. The tubular gas-liquid contact desorber atomization mixing component is a tubular atomizer or a wire mesh packing, and the gas-liquid separation component is a tubular gas-liquid separator.
The method for dehydrating the natural gas glycol by using the efficient compact natural gas glycol dehydration system comprises the following steps:
(1) allowing natural gas with pressure of 2-20MPa to enter a filter separator, removing free liquid water and solid impurities, and discharging from an outlet of the filter separator;
(2) allowing the natural gas discharged in the step (1) to enter a tubular gas-liquid contact absorber, enabling the natural gas to be in parallel flow contact with micron-sized atomized triethylene glycol liquid drops in the tubular gas-liquid contact absorber, discharging the water of the raw material natural gas out of the tubular gas-liquid contact absorber after being absorbed, allowing the water to enter a demister after being cooled by a natural gas/lean glycol heat exchanger, further removing the tiny triethylene glycol liquid drops carried by the natural gas, and discharging the demisted and purified dry natural gas through a demister gas phase outlet to enter a downstream working section;
(3) discharging the rich triethylene glycol absorbing the moisture in the step (2) out of a tubular gas-liquid contact absorber, exchanging heat with triethylene glycol lean solution, then entering a flash tank, flashing the rich triethylene glycol in the flash tank, filtering the rich triethylene glycol through a filter, and then entering a lean/rich ethylene glycol heat exchanger to exchange heat with the lean triethylene glycol;
(4) in the step (3), the triethylene glycol-rich gas enters a tubular gas-liquid contact desorber after heat exchange through a lean/rich glycol heat exchanger, the triethylene glycol-rich gas is atomized into micron-sized liquid drops in the tubular gas-liquid contact desorber and is in countercurrent contact with a stripping agent gasified by a reboiler, and water in the triethylene glycol-rich gas migrates to a gas phase; on one hand, the stripping agent and water in the triethylene glycol form an azeotrope, so that the water is transferred to a gas phase in the form of the azeotrope, on the other hand, the gasified stripping agent can atomize the triethylene glycol into micron-sized liquid drops to increase the gas-liquid mass transfer area, and the triethylene glycol liquid drops and the gasified stripping agent turbulently transfer mass in the same direction, so that the water is promoted to migrate to the gas phase; the desorbed triethylene glycol is discharged from a liquid phase outlet of the tubular gas-liquid contact desorber and enters a reboiler, and the stripping agent is discharged from a gas phase outlet of the tubular gas-liquid contact desorber;
(5) the stripping agent discharged from the gas phase outlet of the tubular gas-liquid contact desorber in the step (4) enters a stripping agent condenser, and is discharged out of the stripping agent condenser after being condensed into a liquid state;
(6) the stripping agent discharged from the stripping agent condenser in the step (5) enters a three-phase separator, water is separated from the stripping agent, the non-condensable gas is led to a tail gas treatment working section, triethylene glycol and water are discharged out of the system, and the stripping agent enters a stripping agent coalescer for coalescence;
(7) in the step (6), the stripping agent is coalesced by a coalescer and then emulsified water in the stripping agent is separated, the coalesced and removed water is discharged out of the system through a bottom outlet, the stripping agent lost in the recovery process of the stripping agent is supplemented through an inlet at the top of the coalescer, and the stripping agent with the emulsified water removed enters a first stripping agent dryer;
(8) the stripping agent entering the first stripping agent dryer in the step (7) sequentially enters the second stripping agent dryer, trace moisture in the stripping agent is further removed through drying, then the stripping agent enters a reboiler, the stripping agent forms an azeotrope with water in triethylene glycol discharged from a liquid phase outlet of the tubular gas-liquid contact desorber in the step (4) in the reboiler, and the azeotrope is gasified, so that the recycling of the stripping agent is realized; the triethylene glycol is discharged from a liquid phase outlet of the reboiler after being further regenerated;
(9) the lean triethylene glycol discharged from the liquid phase outlet of the reboiler in the step (8) enters a lean ethylene glycol storage tank, and a stable liquid level is formed in the storage tank;
(10) and (4) carrying out heat exchange and cooling on the triethylene glycol lean solution in the lean ethylene glycol storage tank in the step (9) by a natural gas/lean ethylene glycol heat exchanger, conveying the triethylene glycol lean solution to a triethylene glycol condenser by a glycol pump, condensing the triethylene glycol condenser, and then feeding the triethylene glycol lean solution into a tubular gas-liquid contact absorber to realize circulation of triethylene glycol.
According to the technical scheme provided by the invention, the efficient and compact natural gas glycol dehydration system and method provided by the embodiment of the invention adopt the tubular gas-liquid contact absorber to replace a rectification column of a traditional glycol regeneration system, so that the compactness of the natural gas glycol dehydration system is further enhanced, and the flexibility of the installation and arrangement of a dehydration device is improved. The whole device has light weight, small occupied area, low glycol circulation amount and flexible installation and arrangement, and the dehydrated natural gas water dew point meets the requirements of offshore platform production and long-distance gathering and transportation indexes. The problem that the existing natural gas triethylene glycol dehydration process technology adopting the traditional tower type mass transfer device is applied to an offshore platform is solved.
Drawings
FIG. 1 is a diagram of the efficient compact natural gas glycol dehydration process of the present invention;
FIG. 2 is a schematic structural view of a tubular gas-liquid contact mass transfer device adopting a tubular atomizer structure according to the present invention;
FIG. 3 is a schematic structural diagram of a tubular gas-liquid contact mass transfer device adopting a wire mesh packing structure according to the present invention;
in the figure:
1-a filter separator underflow valve, 2-a filter separator, 3-a tubular gas-liquid contact absorber, 4-a triethylene glycol condenser, 5-a glycol pump, 6-a natural gas/lean glycol heat exchanger, 7-a demister, 8-a demister underflow valve, 9-a lean glycol storage tank, 10-a lean/rich glycol heat exchanger, 11-a tubular gas-liquid contact desorber, 12-a condenser, 13-a three-phase separator, 14-a stripping agent pump, 15-a first stop valve, 16-a stripping agent injection stop valve, 17-a coalescer, 18-a coalescer drain valve, 19-a first stripping agent dryer, 20-a second stripping agent dryer, 21-a stripping agent heater, 22-a reboiler, 23-a glycol filter, 24-a flash tank, 25-second stop valve.
Detailed Description
The embodiments of the present invention will be described in further detail below. Details which are not described in detail in the embodiments of the invention belong to the prior art which is known to the person skilled in the art.
The high-efficiency compact natural gas glycol dehydration system of the invention has the preferred embodiment as shown in fig. 1 to 3:
the device comprises a filtering separator underflow valve 1, a filtering separator 2, a tubular gas-liquid contact absorber 3, a triethylene glycol condenser 4, a glycol pump 5, a natural gas/lean glycol heat exchanger 6, a demister 7, a demister underflow valve 8, a lean glycol storage tank 9, a lean/rich glycol heat exchanger 10, a tubular gas-liquid contact desorber 11, a condenser 12, a three-phase separator 13, a stripping agent pump 14, a first stop valve 15, a stripping agent injection stop valve 16, a coalescer 17, a coalescer drain valve 18, a first stripping agent dryer 19, a second stripping agent dryer 20, a stripping agent heater 21, a reboiler 22, a glycol filter 23, a flash tank 24 and a second stop valve 25 which are connected through pipelines;
the bottom outlet of the filter separator 2 is connected with a filter separator underflow valve 1, the outlet of the filter separator underflow valve 1 is connected with a downstream sewage disposal system, and the top outlet of the filter separator 2 is connected with a gas phase inlet of a tubular gas-liquid contact absorber 3;
a gas phase outlet of the tubular gas-liquid contact absorber 3 is connected with a natural gas inlet of a natural gas/lean glycol heat exchanger 6, a natural gas outlet of the natural gas/lean glycol heat exchanger 6 is connected with an inlet of a demister 7, a gas phase outlet at the upper part of the demister 7 is connected with a downstream natural gas treatment section, a liquid phase outlet at the lower part of the demister 7 is connected with an inlet of a demister underflow valve 8, and an outlet of the demister underflow valve 8 is connected with a flash tank 24;
a liquid phase outlet at the lower part of the tubular gas-liquid contact absorber 3 is connected with a second stop valve 25, the second stop valve 25 is connected with a flash drum 24, a gas phase outlet at the upper part of the flash drum 24 is connected with a tail gas treatment system, a liquid phase outlet at the bottom of the flash drum 24 is connected with an inlet of a glycol filter 23, an outlet of the glycol filter 23 is connected with a glycol-rich inlet of the lean/glycol-rich heat exchanger 10, a glycol-rich outlet of the lean/glycol-rich heat exchanger 10 is connected with a liquid phase inlet of the tubular gas-liquid contact desorber 11, and a liquid phase outlet of the tubular gas-liquid contact desorber 11 is connected with an inlet at the upper part of the reboiler 22;
a gas phase outlet of the tubular gas-liquid contact desorber 11 is connected with an inlet of a condenser 12, an outlet of the condenser 12 is connected with an inlet of a three-phase separator 13, a non-condensable gas outlet of the three-phase separator 13 leads to tail gas treatment, and a water outlet is arranged at the lower end of the three-phase separator 13;
the outlet of the stripping agent of the three-phase separator 13 is connected with the inlet of a stripping agent pump 14, the outlet of the stripping agent pump 14 is connected with the inlet of a stripping agent coalescer 17, the outlet of the stripping agent coalescer 17 is connected with the inlet of a first stripping agent dryer 19, the upper part of the stripping agent coalescer 17 is provided with a stripping agent feeding port and is connected with a stripping agent injection stop valve 16, the stripping agent is fed through the inlet of the stripping agent injection stop valve 16, and the lower part of the stripping agent coalescer 17 is provided with a water drain port and is connected with a coalescer drain valve 18;
the first stripping agent dryer 19, the second stripping agent dryer 20 and the stripping agent heater 21 are sequentially connected, and an outlet of the stripping agent heater 21 is connected with a stripping agent inlet at the lower part of the reboiler 22 to realize circulation of the stripping agent;
the gas phase outlet of the reboiler 22 is connected with the gas phase inlet of the tubular gas-liquid contact desorber 11, the liquid phase outlet of the reboiler 22 is connected with the lean glycol inlet of the lean/rich glycol heat exchanger 6, the lean glycol outlet of the lean/rich glycol heat exchanger 6 is connected with the inlet of the lean glycol storage tank 9, the bottom outlet of the lean glycol storage tank 9 is connected with the lean glycol inlet of the natural gas/lean glycol heat exchanger 6, the lean glycol outlet of the natural gas/lean glycol heat exchanger 9 is connected with the inlet of the glycol pump 5, the outlet of the glycol pump 5 is connected with the inlet of the triethylene glycol condenser 4, and the outlet of the triethylene glycol condenser 4 is connected with the liquid phase inlet of the tubular gas-liquid contact absorber 3, so that the circulation of the triethylene glycol is realized.
The tubular gas-liquid contact absorber is characterized in that the atomizing part is a tubular atomizer or a wire mesh packing, and the gas-liquid separation part is a demisting tubular gas-liquid separator. The tubular gas-liquid contact desorber atomization mixing component is a tubular atomizer or a wire mesh packing, and the gas-liquid separation component is a tubular gas-liquid separator.
The method for dehydrating the natural gas glycol by using the efficient compact natural gas glycol dehydration system comprises the following steps:
(1) allowing natural gas with pressure of 2-20MPa to enter a filter separator, removing free liquid water and solid impurities, and discharging from an outlet of the filter separator;
(2) allowing the natural gas discharged in the step (1) to enter a tubular gas-liquid contact absorber, enabling the natural gas to be in parallel flow contact with micron-sized atomized triethylene glycol liquid drops in the tubular gas-liquid contact absorber, discharging the water of the raw material natural gas out of the tubular gas-liquid contact absorber after being absorbed, allowing the water to enter a demister after being cooled by a natural gas/lean glycol heat exchanger, further removing the tiny triethylene glycol liquid drops carried by the natural gas, and discharging the demisted and purified dry natural gas through a demister gas phase outlet to enter a downstream working section;
(3) discharging the rich triethylene glycol absorbing the moisture in the step (2) out of a tubular gas-liquid contact absorber, exchanging heat with triethylene glycol lean solution, then entering a flash tank, flashing the rich triethylene glycol in the flash tank, filtering the rich triethylene glycol through a filter, and then entering a lean/rich ethylene glycol heat exchanger to exchange heat with the lean triethylene glycol;
(4) in the step (3), the triethylene glycol-rich gas enters a tubular gas-liquid contact desorber after heat exchange through a lean/rich glycol heat exchanger, the triethylene glycol-rich gas is atomized into micron-sized liquid drops in the tubular gas-liquid contact desorber and is in countercurrent contact with a stripping agent gasified by a reboiler, and water in the triethylene glycol-rich gas migrates to a gas phase; on one hand, the stripping agent and water in the triethylene glycol form an azeotrope, so that the water is transferred to a gas phase in the form of the azeotrope, on the other hand, the gasified stripping agent can atomize the triethylene glycol into micron-sized liquid drops to increase the gas-liquid mass transfer area, and the triethylene glycol liquid drops and the gasified stripping agent turbulently transfer mass in the same direction, so that the water is promoted to migrate to the gas phase; the desorbed triethylene glycol is discharged from a liquid phase outlet of the tubular gas-liquid contact desorber and enters a reboiler, and the stripping agent is discharged from a gas phase outlet of the tubular gas-liquid contact desorber;
(5) the stripping agent discharged from the gas phase outlet of the tubular gas-liquid contact desorber in the step (4) enters a stripping agent condenser, and is discharged out of the stripping agent condenser after being condensed into a liquid state;
(6) the stripping agent discharged from the stripping agent condenser in the step (5) enters a three-phase separator, water is separated from the stripping agent, the non-condensable gas is led to a tail gas treatment working section, triethylene glycol and water are discharged out of the system, and the stripping agent enters a stripping agent coalescer for coalescence;
(7) in the step (6), the stripping agent is coalesced by a coalescer and then emulsified water in the stripping agent is separated, the coalesced and removed water is discharged out of the system through a bottom outlet, the stripping agent lost in the recovery process of the stripping agent is supplemented through an inlet at the top of the coalescer, and the stripping agent with the emulsified water removed enters a first stripping agent dryer;
(8) the stripping agent entering the first stripping agent dryer in the step (7) sequentially enters the second stripping agent dryer, trace moisture in the stripping agent is further removed through drying, then the stripping agent enters a reboiler, the stripping agent forms an azeotrope with water in triethylene glycol discharged from a liquid phase outlet of the tubular gas-liquid contact desorber in the step (4) in the reboiler, and the azeotrope is gasified, so that the recycling of the stripping agent is realized; the triethylene glycol is discharged from a liquid phase outlet of the reboiler after being further regenerated;
(9) the lean triethylene glycol discharged from the liquid phase outlet of the reboiler in the step (8) enters a lean ethylene glycol storage tank, and a stable liquid level is formed in the storage tank;
(10) and (4) carrying out heat exchange and cooling on the triethylene glycol lean solution in the lean ethylene glycol storage tank in the step (9) by a natural gas/lean ethylene glycol heat exchanger, conveying the triethylene glycol lean solution to a triethylene glycol condenser by a glycol pump, condensing the triethylene glycol condenser, and then feeding the triethylene glycol lean solution into a tubular gas-liquid contact absorber to realize circulation of triethylene glycol.
The volume ratio of the triethylene glycol barren solution to the natural gas in the step (2) is 1:500-1: 10000.
The volume ratio of the triethylene glycol rich solution to the gaseous stripping agent in the step (4) is 1:50-1: 1000.
The flow velocity of natural gas in the tubular gas-liquid contact absorber in the step (2) is 6-30 m/s, the D32 particle size of the atomized triethylene glycol-poor liquid drops is 5-200 mu m, the gas phase flow velocity in the tubular gas-liquid contact desorber in the step (4) is 6-30 m/s, and the D32 particle size of the atomized triethylene glycol-rich liquid drops is 5-200 mu m.
In the step (4), the stripping agent is one or more of isooctane, n-heptane, toluene, ethylbenzene and the like which can form a low-boiling-point azeotrope with water.
In the step (8) and the step (9), the heating temperature in the reboiler is 195 ℃ -204 ℃.
In the step (10), the temperature of the triethylene glycol condenser is 15-40 ℃.
The method is used for dehydrating natural gas glycol in an offshore gas field.
The tubular gas-liquid contact absorber for gas-liquid parallel flow contact absorption and mass transfer enhancement is compact and efficient gas-liquid contact absorption equipment, replaces a traditional absorption tower in a natural gas dehydration process method, and can obviously reduce the space and the weight of a natural gas dehydration treatment device. The glycol is atomized into small drops in the glycol rectification regeneration process, and the gas-liquid mass transfer process of the regeneration system can also be enhanced.
The efficient compact natural gas glycol dehydration system and the method improve the natural gas glycol dehydration system in the prior art, adopt the tubular gas-liquid contact absorber to replace a rectifying column of a traditional glycol regeneration system, further enhance the compactness of the natural gas glycol dehydration system and improve the flexibility of the installation and the arrangement of a dehydration device. The whole device has light weight, small occupied area, low glycol circulation amount and flexible installation and arrangement, and the dehydrated natural gas water dew point meets the requirements of offshore platform production and long-distance gathering and transportation indexes. The problem that the existing natural gas triethylene glycol dehydration process technology adopting the traditional tower type mass transfer device is applied to an offshore platform is solved.
The absorption and regeneration processes of the invention both adopt tubular gas-liquid mass transfer equipment based on micro-droplet gas-liquid parallel flow enhanced mass transfer, and combine the technical advantages of the natural gas dehydration technology by the triethylene glycol method, thus not only ensuring that the water dew point of the gas outlet is maintained in the required range when the flow fluctuation of the gas inlet is large, leading the water dew point of the outlet to reach the standard requirement of gathering or downstream processing technology, but also simplifying the natural gas glycol dehydration system. The requirements of the offshore platform on the size and the weight of the equipment can be met by utilizing the characteristics of high mass transfer efficiency, light weight, small occupied area and flexible installation and arrangement of the tubular gas-liquid contact mass transfer equipment.
The triethylene glycol solution has the advantages of good thermal stability, high boiling point, low steam pressure, easiness in regeneration, high hygroscopicity, small carrying loss, reliability in operation and the like, and the gas-liquid contact mass transfer process is strengthened by utilizing the parallel flow of the atomized micron-sized triethylene glycol liquid drops and the high-speed gas flow in the tubular gas-liquid contact absorber and the tubular gas-liquid contact desorber.
The natural gas dehydration process of the tubular gas-liquid contact mass transfer device based on the micro-droplet gas-liquid parallel flow enhanced mass transfer has the advantages of large treatment capacity and high efficiency, has a large treatment range of liquid-gas ratio, can still achieve an ideal dehydration effect at a low liquid-gas ratio, reduces the consumption of triethylene glycol, and thus saves the energy consumption of a glycol regeneration device. The absorption equipment and the regeneration device both adopt a tubular gas-liquid contact mass transfer device, and the gas-liquid contact mass transfer device can reach the feed gas dehydration balance degree and the outlet water dew point which are difficult to reach by tower-type gas-liquid mass transfer equipment. In addition, the water content, namely the dehydration balance degree, of the outlet gas and the dew point of the outlet gas can be effectively controlled by regulating the injection amount of the glycol liquid and the particle size of the atomized liquid drops. Therefore, the preferable conditions make the natural gas-glycol dehydration process of the tubular gas-liquid contact mass transfer device based on micro-droplet gas-liquid cocurrent flow reinforced contact mass transfer far superior to the traditional tower dehydration process.
The invention has the following beneficial effects:
1) the tubular gas-liquid contact absorption dehydration device comprises a tubular atomization component and a tubular gas-liquid separator, wherein the tubular atomization component atomizes glycol lean solution into micron-sized liquid drops in high-speed gas flow, and the high-speed gas flow and the micron-sized liquid drops form a gas-liquid high-dispersion system in a contact mass transfer pipe section, so that the gas-liquid contact area is remarkably increased, the gas-liquid absorption mass transfer dehydration effect is improved, and the dehydration efficiency is higher;
2) the tubular gas-liquid contact dehydration regeneration device comprises a tubular atomization component and a tubular gas-liquid separator, the tubular atomization component atomizes glycol rich liquid into micron-sized liquid drops in high-speed gas flow, the high-speed gas flow and the micron-sized liquid drops form a gas-liquid high-dispersion system in a contact mass transfer pipe section, the gas-liquid contact area is remarkably increased, so that moisture in the glycol rich liquid drops is volatilized as far as possible, triethylene glycol lean solution is obtained through regeneration, and the glycol regeneration efficiency is higher;
3) the glycol liquid holdup in the tubular gas-liquid contact mass transfer equipment is low, the gas-liquid contact mass transfer efficiency of a gas-liquid high dispersion system formed by micron-sized liquid drops is high, and the dehydration system designed by adopting the tubular gas-liquid contact mass transfer process has the advantage of low glycol circulation amount, can obviously reduce the energy consumption of glycol regeneration, and is more beneficial to industrial application.
4) By combining the natural gas dehydration process of the tubular gas-liquid contact mass transfer enhancement based on the micro-droplet high-dispersion tubular gas-liquid contact mass transfer dehydration and regeneration device, the flash tank and the reboiler in the technology, the organic combination of the tubular micro-droplet enhancement gas-liquid mass transfer technology, the traditional triethylene glycol dehydration tower process and the ethylene glycol rectification column regeneration process is realized. Compared with the dehydration process adopting the traditional tower-type gas-liquid contact mass transfer equipment, the whole process has the characteristics of high absorption mass transfer efficiency, low outlet dew point, light weight of the equipment, small occupied area, flexible installation and arrangement, high system robustness and the like.
The specific embodiment is as follows:
referring to fig. 1, the invention provides a high-efficiency compact natural gas glycol dehydration process, which comprises a filter separator underflow valve 1, a filter separator 2, a tubular gas-liquid contact absorber 3, a triethylene glycol condenser 4, a glycol pump 5, a natural gas/lean glycol heat exchanger 6, a demister 7, a demister underflow valve 8, a lean glycol storage tank 9, a lean/rich glycol heat exchanger 10, a tubular gas-liquid contact desorber 11, a condenser 12, a three-phase separator 13, a stripping agent pump 14, a first stop valve 15, a stripping agent injection stop valve 16, a coalescer 17, a coalescer drain valve 18, a first stripping agent dryer 19, a second stripping agent dryer 20, a stripping agent heater 21, a reboiler 22, a glycol filter 23, a flash tank 24 and a second stop valve 25.
The bottom outlet of the filter separator 2 is connected with a filter separator underflow valve 1, the outlet of the filter separator underflow valve 1 is connected with a downstream sewage disposal system, and the top outlet of the filter separator 2 is connected with a gas phase inlet of a tubular gas-liquid contact absorber 3;
the gas phase outlet of the tubular gas-liquid contact absorber 3 is connected with the natural gas inlet of the natural gas/lean glycol heat exchanger 6, the natural gas outlet of the natural gas/lean glycol heat exchanger 6 is connected with the inlet of a demister 7, the gas phase outlet at the upper part of the demister 7 is connected with a downstream natural gas treatment section, the liquid phase outlet at the lower part of the demister 7 is connected with the inlet of a demister underflow valve 8, and the outlet of the demister underflow valve 8 is connected with a flash tank 24.
A liquid phase outlet at the lower part of the tubular gas-liquid contact absorber 3 is connected with a second stop valve 25, the second stop valve 25 is connected with a flash drum 24, a gas phase outlet at the upper part of the flash drum 24 is connected with a tail gas treatment system, a liquid phase outlet at the bottom of the flash drum 24 is connected with an inlet of a glycol filter 23, an outlet of the glycol filter 23 is connected with a glycol-rich inlet of the lean/glycol-rich heat exchanger 10, a glycol-rich outlet of the lean/glycol-rich heat exchanger 10 is connected with a liquid phase inlet of the tubular gas-liquid contact desorber 11, and a liquid phase outlet of the tubular gas-liquid contact desorber 11 is connected with an inlet at the upper part of the reboiler 22;
a gas phase outlet of the tubular gas-liquid contact desorber 11 is connected with an inlet of a condenser 12, an outlet of the condenser 12 is connected with an inlet of a three-phase separator 13, a non-condensable gas outlet of the three-phase separator 13 leads to tail gas treatment, and a water outlet is arranged at the lower end of the three-phase separator 13;
the outlet of the stripping agent of the three-phase separator 13 is connected with the inlet of a stripping agent pump 14, the outlet of the stripping agent pump 14 is connected with the inlet of a stripping agent coalescer 17, the outlet of the stripping agent coalescer 17 is connected with the inlet of a first stripping agent dryer 19, the upper part of the stripping agent coalescer 17 is provided with a stripping agent feeding port and is connected with a stripping agent injection stop valve 16, and the stripping agent is fed through the inlet of the stripping agent injection stop valve 16. The lower part of the stripping agent coalescer 17 is provided with a water discharge port connected with a coalescer water discharge valve 18.
The first stripping agent dryer 19, the second stripping agent dryer 20 and the stripping agent heater 21 are sequentially connected, and an outlet of the stripping agent heater 21 is connected with a stripping agent inlet at the lower part of the reboiler 22, so that the circulation of the stripping agent is realized.
The gas phase outlet of the reboiler 22 is connected with the gas phase inlet of the tubular gas-liquid contact desorber 11, the liquid phase outlet of the reboiler 22 is connected with the lean glycol inlet of the lean/rich glycol heat exchanger 6, the lean glycol outlet of the lean/rich glycol heat exchanger 6 is connected with the inlet of the lean glycol storage tank 9, the bottom outlet of the lean glycol storage tank 9 is connected with the lean glycol inlet of the natural gas/lean glycol heat exchanger 6, the lean glycol outlet of the natural gas/lean glycol heat exchanger 9 is connected with the inlet of the glycol pump 5, the outlet of the glycol pump 5 is connected with the inlet of the triethylene glycol condenser 4, and the outlet of the triethylene glycol condenser 4 is connected with the liquid phase inlet of the tubular gas-liquid contact absorber 3, so that the circulation of the triethylene glycol is realized.
The invention utilizes the process for carrying out the compact and high-efficiency tubular triethylene glycol method natural gas dehydration based on the micro-droplet reinforced gas-liquid mass transfer, which comprises the following steps:
(1) allowing natural gas with pressure of 2-20MPa to enter a filter separator, removing free liquid water and solid impurities, and discharging from an outlet of the filter separator;
(2) allowing the natural gas discharged in the step (1) to enter a tubular gas-liquid contact absorber, enabling the natural gas to be in parallel flow contact with micron-sized atomized triethylene glycol liquid drops in the tubular gas-liquid contact absorber, discharging the water of the raw gas out of the tubular gas-liquid contact absorber after being absorbed, allowing the water to enter a demister after being cooled by a natural gas/lean glycol heat exchanger, further removing the tiny triethylene glycol liquid drops carried by the natural gas, and discharging the demisted and purified dry natural gas through a demister gas phase outlet to enter a downstream working section;
(3) discharging the rich triethylene glycol absorbing the moisture in the step (2) out of a tubular gas-liquid contact absorber, exchanging heat with triethylene glycol lean solution, then entering a flash tank, flashing the rich triethylene glycol in the flash tank, filtering the rich triethylene glycol through a filter, and then entering a lean/rich ethylene glycol heat exchanger to exchange heat with the lean triethylene glycol;
(4) in the step (3), the triethylene glycol-rich gas enters a tubular gas-liquid contact desorber after heat exchange through a lean/rich glycol heat exchanger, the triethylene glycol-rich gas is atomized into micron-sized liquid drops in the tubular gas-liquid contact desorber and is in countercurrent contact with a stripping agent gasified by a reboiler, and water in the triethylene glycol-rich gas migrates to a gas phase; on one hand, the stripping agent and water in the triethylene glycol form an azeotrope, so that the water is transferred to a gas phase in the form of the azeotrope, on the other hand, the gasified stripping agent can atomize the triethylene glycol into micron-sized liquid drops to increase the gas-liquid mass transfer area, and the triethylene glycol liquid drops and the gasified stripping agent turbulently transfer mass in the same direction, so that the water is promoted to migrate to the gas phase; the desorbed triethylene glycol is discharged from a liquid phase outlet of the tubular gas-liquid contact desorber and enters a reboiler, and the stripping agent is discharged from a gas phase outlet of the tubular gas-liquid contact desorber;
(5) the stripping agent discharged from the gas phase outlet of the tubular gas-liquid contact desorber in the step (4) enters a stripping agent condenser, and is discharged out of the stripping agent condenser after being condensed into a liquid state;
(6) the stripping agent discharged from the stripping agent condenser in the step (5) enters a three-phase separator, water is separated from the stripping agent, the non-condensable gas is led to a tail gas treatment working section, triethylene glycol and water are discharged out of the system, and the stripping agent enters a stripping agent coalescer for coalescence;
(7) in the step (6), the stripping agent is coalesced by a coalescer and then emulsified water in the stripping agent is separated, the coalesced and removed water is discharged out of the system through a bottom outlet, the stripping agent lost in the recovery process of the stripping agent is supplemented through an inlet at the top of the coalescer, and the stripping agent with the emulsified water removed enters a first stripping agent dryer;
(8) the stripping agent entering the first stripping agent dryer in the step (7) sequentially enters the second stripping agent dryer, trace moisture in the stripping agent is further removed through drying, then the stripping agent enters a reboiler, the stripping agent forms an azeotrope with water in triethylene glycol discharged from a liquid phase outlet of the tubular gas-liquid contact desorber in the step (4) in the reboiler, and the azeotrope is gasified, so that the recycling of the stripping agent is realized; the triethylene glycol is discharged from a liquid phase outlet of the reboiler after being further regenerated;
(9) the lean triethylene glycol discharged from the liquid phase outlet of the reboiler in the step (8) enters a lean ethylene glycol storage tank, and a stable liquid level is formed in the storage tank;
(10) and (4) carrying out heat exchange and cooling on the triethylene glycol lean solution in the lean ethylene glycol storage tank in the step (9) by a natural gas/lean ethylene glycol heat exchanger, conveying the triethylene glycol lean solution to a triethylene glycol condenser by a glycol pump, condensing the triethylene glycol condenser, and then feeding the triethylene glycol lean solution into a tubular gas-liquid contact absorber to realize circulation of triethylene glycol.
In certain embodiments of the invention, the volume ratio of triethylene glycol to natural gas in step (2) is from 1:500 to 1: 10000.
In certain embodiments of the present invention, in step (2), the triethylene glycol lean solution concentration can reach 99.99%, the equilibrium degree of dehydration of the natural raw material gas reaches more than 95%, and the outlet dew point reaches below-60 ℃.
In some embodiments of the invention, the tubular gas-liquid contact absorber atomization component in step (2) is a tubular atomizer or a wire mesh packing, the gas-liquid separation component is a demisting type tubular gas-liquid separator,
in certain embodiments of the present invention, the tubular gas-liquid contact desorber atomizing and mixing component in step (4) is a tubular atomizer or a wire mesh packing, and the gas-liquid separation component is a tubular gas-liquid separator.
In certain embodiments of the invention, the volume ratio of triethylene glycol rich to gaseous stripping agent in step (4) is from 1:50 to 1: 1000.
In some embodiments of the present invention, the flow rate of the natural gas in the tubular gas-liquid contact absorber in step (2) is 6 to 30m/s, the particle size of D32 of the atomized triethylene glycol-poor liquid droplets is 5 to 200 μm, the flow rate of the gas phase in the tubular gas-liquid contact desorber in step (4) is 6 to 30m/s, and the particle size of D32 of the atomized triethylene glycol-rich liquid droplets is 5 to 200 μm.
In certain embodiments of the present invention, the stripping agent in step (4) is one or more of isooctane, n-heptane, toluene, ethylbenzene, etc., which can form a low boiling azeotrope with water.
In certain embodiments of the invention, the reboiler temperature in steps (8) and (9) is 195 ℃ to 204 ℃.
In certain embodiments of the invention, in step (10), the temperature of the triethylene glycol condenser is between 15 ℃ and 40 ℃.
Example 1
The above apparatus and process were used to remove gaseous water from natural gas with triethylene glycol:
the natural gas pressure entering the system is 7MPa, the volume ratio of the triethylene glycol lean solution to the natural gas to be treated is 1:10000, the volume ratio of the using amount of a stripping agent to the using amount of the triethylene glycol rich solution is 0.15:1, the stripping agent is n-heptane, the temperature of a triethylene glycol condenser is 35 ℃, the natural gas flow rate in a tubular gas-liquid contact absorber is 12m/s, the particle size of triethylene glycol lean solution atomized liquid drops D32 is 100 mu m, the gas flow rate in the tubular gas-liquid contact desorber is 12m/s, the particle size of triethylene glycol rich solution atomized liquid drops D32 is 100 mu m, and the temperature of a reboiler is 204 ℃; under the process condition, the purity of the regenerated triethylene glycol barren solution reaches 99.99 wt%, and the water dew point of the dehydrated natural gas reaches-60 ℃.
Example 2
As shown in example 1, other conditions are unchanged, the flow rate of the natural gas in the tubular gas-liquid contact absorber is 20m/s, the particle size of the atomized droplets D32 of the triethylene glycol lean solution is 60 μm, the flow rate of the gas phase in the tubular gas-liquid contact desorber is 20m/s, and the particle size of the atomized droplets D32 of the triethylene glycol rich solution is 60 μm, so that the purity of the regenerated triethylene glycol lean solution reaches 99.99 wt%, and the water dew point of the dehydrated natural gas reaches-70 ℃.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are included in the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
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