CN106583066A - Low-temperature cyclone supersonic separation device and natural gas dehydration and dehydrocarbon process - Google Patents
Low-temperature cyclone supersonic separation device and natural gas dehydration and dehydrocarbon process Download PDFInfo
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- CN106583066A CN106583066A CN201611117414.8A CN201611117414A CN106583066A CN 106583066 A CN106583066 A CN 106583066A CN 201611117414 A CN201611117414 A CN 201611117414A CN 106583066 A CN106583066 A CN 106583066A
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- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 31
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 16
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- 239000002994 raw material Substances 0.000 claims abstract description 12
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- 239000002808 molecular sieve Substances 0.000 description 6
- 238000005057 refrigeration Methods 0.000 description 6
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 6
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- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
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- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- 230000006911 nucleation Effects 0.000 description 1
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- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C3/00—Apparatus in which the axial direction of the vortex flow following a screw-thread type line remains unchanged ; Devices in which one of the two discharge ducts returns centrally through the vortex chamber, a reverse-flow vortex being prevented by bulkheads in the central discharge duct
-
- 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
-
- 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
Abstract
The invention belongs to the technical field of treatment of natural gas, and in particular, relates to a low-temperature cyclone supersonic separation device and a natural gas dehydration and dehydrocarbon process. The process comprises the following steps: raw material gas of natural gas is cooled by a heat exchanger to enter a NGsd device for high-speed cyclone in the NGsd device, expansion pressure reduction in a spraying pipe, cooling, acceleration and separation to obtain a gas-liquid mixture of water and light hydrocarbon and dry gas; and the obtained water and light hydrocarbon gas-liquid mixture enters a gas-liquid separator for separation to obtain water and light hydrocarbon and shunted dry gas. The device and the process are high in natural gas dehydration and dehydrocarbon efficiency and low in energy consumption, integrate such functions as cooling, gas-liquid separation and once generation of the dry gas as a whole, are applied to the gas treatment process flow, can reduce equipment and realize real short flow, and save the investment cost.
Description
Technical field
The invention belongs to natural gas processing technical field, and in particular to low temperature spiral-flow type supersonic speed separator and natural gas
Dehydration hydrocarbon removal process.
Background technology
The de- hydrocarbon of gas dehydration is requisite link during natural gas purification, selects suitable dehydration, de- hydrocarbon skill
Art and technique are very important.At present, the commonly used conventional natural gas dehydration of domestic and international oil gas field, de- hydrocarbon technology, mainly
Including solvent absorption, solid absorption method, freezing separation method etc., the wherein commercial Application of chemical reaction method is few, and solvent is inhaled
Receipts method and solid absorption method application are extremely wide.
Solvent absorption technology：By the use of with very strong absorptive alcohol compound as absorbent, such as ethylene glycol, two sweet
Alcohol and triethylene glycol (TEG).It is wherein more preferable with the heat endurance of triethylene glycol, and it is easy to regeneration, steam is forced down, and carries loss amount more
It is little, so using in a large number.This dewatering system includes separator, absorption tower and triethylene glycol regenerative system, applies absorption, divides
From, gas-liquid contact, mass transfer, the technological principle such as heat transfer and extracting, depoint depression can reach 30～60 DEG C.At present, triethylene glycol dehydration
The subject matter for facing has：Systematic comparison complexity, triethylene glycol. solution regeneration energy consumption is big, there is loss, contaminated, oxidation and generates corruption
The problems such as corrosion organic acid, equipment takes up space greatly, and plant maintenance is complicated.Above reason causes triethylene glycol evaporation to invest and transport
Row high cost, and with plant running time lengthening, triethylene glycol consumption gradually increases, therefore triethylene glycol consumption becomes shadow
Ring the key factor of production cost.
Solid absorption technology：It is dehydrated using solid absorbent, it is conventional to have silica gel, activated alumina, molecular sieve.Molecular sieve
There are more advantages, thus be used widely.Molecular sieve dehydration system mainly includes that 2 or 3 are in dehydration, regenerate and cold
The drier of state, and regeneration gas heating system are blown, more suitable for deep dehydration, dew point can be reduced to less than -73 DEG C.But
The subject matter of molecular sieve dehydration is that equipment investment and Operation cost comparison are high, and regenerating molecular sieve energy consumption is big, and in natural gas
Heavy hydrocarbon, H2S and CO2Pollute etc. solid absorbent can be made.In addition, the regenerative process observable index of molecular sieve dehydration is larger, drier
The adsorbent of lower floor needs Jing often to change.
Freezing separation technology：Freezing separation technology includes direct cooling method, pressurization cooling method, throttling expansion refrigeration and machinery
The methods such as refrigeration.The de- hydrocarbon of J-T valves and turbo-expander belongs to the de- hydrocarbon of cryogenic condensation method, with flow process is simple, cost is low excellent
Point, the method be in domestic gas field in addition to triethylene glycol method apply more natural gas dehydration process.It is particularly suitable for high pressure gas
Body, but when gas pressure is not enough, outer defeated requirement is not reached using the dehydration of freezing separation method, and be pressurized or outside introducing low-temperature receiver
When uneconomical, then other dewaterings must be adopted.The current subject matter of the method is power consumption height, water dew point height etc..And,
Turbo-expander has high-speed moving part, and manufacture difficulty is big, poor reliability.
Gas dehydration and lighter hydrocarbons separation are the important process links of oil gas field surface production, and above-mentioned traditional low temperature point
Separating process low separation efficiency, investment and operating cost are high, heating and anti-freezing is difficult, antifreezing agent consumption is big.Propose for problems
Exempt from that to heat or exempt from the low temperature spiral-flow type supersonic speed separation technology for filling antifreezing agent be the big of natural gas processing technology
Innovation.2011, Tarim Oilfield tooth breathed out the first low temperature spiral-flow type supersonic speed that operation area adopts now in gas dehydration
Separation removal device, and succeed.
By multi-specialized synthesis such as machinery, physics, technique, the equipment involved by gas dehydration supersonic speed isolation technics
Research, solves olefin treated, antifreeze consumption, can process that tolerance is limited to wait technical barrier, and research and development adapt to offshore platform environment, big
Width mitigates platform to be born a heavy burden, reduces occupation area of equipment, can process the natural gas dehydration technique containing high acid gas, is organized and implemented super
The large-scale promotion application of velocity of sound isolation technics, is that " 13 " improve gas dehydration efficiency, energy saving and cost lowering in oilfield construction
Synergy provides technical support.
The content of the invention
First technical problem to be solved by this invention is to provide a kind of low temperature spiral-flow type supersonic speed separator, the dress
Put including gas access, impeller inducer cyclone, supersonic speed Rafael nozzle, separate back taper, boosting diffuser, liquid outlet,
Gas vent composition after separation.
Further, in above-mentioned low temperature spiral-flow type supersonic speed separator, the supersonic speed De Laval noz(zle) is divided into four
Point：Stable section, subsonic speed contraction section, throat, supersonic speed expansion segment.
Second technical problem to be solved by this invention is to provide gas dehydration hydrocarbon removal process, the technique include with
Lower step：
(1), natural gas _ raw material gas into NGsd devices, and revolve in NGsd devices Jing after heat exchanger cooling through high speed
Flow, expand in jet pipe gas-liquid mixture, the dry gas of step-down, cooling and speedup, isolated water and lighter hydrocarbons；
(2) water and the gas-liquid mixture of lighter hydrocarbons that, step (1) obtains enters gas-liquid separator, isolated water and
Lighter hydrocarbons, shunting dry gas.
Wherein, above-mentioned gas dehydration hydrocarbon removal process also includes step (3)：Dry gas and step that the step (1) obtains
(2) the shunting dry gas for obtaining, Jing gas mixers mixing, is recycled into the heat exchanger, outer defeated after exchanging heat with natural gas _ raw material gas,
Obtain dry gas product.
Wherein, in above-mentioned gas dehydration hydrocarbon removal process step (1), the natural gas _ raw material gas are Jing after heat exchanger cooling
Temperature is -80 DEG C.
Wherein, in above-mentioned gas dehydration hydrocarbon removal process step (1), the high-speed rotational produce tangential acceleration be l ×
106m/s2Eddy flow.
Wherein, in above-mentioned gas dehydration hydrocarbon removal process step (1), the raw natural gas produce temperature Jing after high-speed rotational
Degree 20 DEG C, the saturated natural gas of pressure 10MPa.
Wherein, in above-mentioned gas dehydration hydrocarbon removal process step (1), the speed ＞ 550m/s after the speedup.
Wherein, the NGsd devices are the abbreviation of the low temperature spiral-flow type supersonic speed separator.
The invention has the beneficial effects as follows：
(1) efficiency high：There is step-down, cooling, speedup in low temperature spiral-flow type supersonic speed separator supersonic nozzle
Process, and occur at jet pipe rear portion to diffuser deceleration, boosting, temperature-rise period, all it is the conversion of gas interior energy, do not exist
Energy ezpenditure and loss.Therefore, the separator for being manufactured using low temperature spiral-flow type supersonic speed separation removal technology not only compares constant enthalpy
The J-T valve efficiency highs of throttling expansion refrigeration, and it is higher than the efficiency of expander of constant entropy throttling expansion；
(2) energy consumption is low：NGL (NGL is lighter hydrocarbons, refers to the liquid hydrocarbon mixture being recovered to from natural gas, including ethane,
Propane, butane and pentane above hydro carbons) in the case of yield identical, using low temperature spiral-flow type supersonic speed separator with use J-
T valves are compared, and the separator manufactured using low temperature spiral-flow type supersonic speed separation removal technology can reduce power consumption 50%～70%；With
Separator substitutes decompressor and can reduce work done during compression 15%～20%.Particularly when decompressor is due to technical reason (such as import
Pressure is too high), or use the uneconomic occasion of decompressor, the advantage of low temperature spiral-flow type supersonic speed separator in middle small field
More project；
(3) the separator no-rotary part manufactured using low temperature spiral-flow type supersonic speed separation removal technology, belongs to static equipment,
Not only maintenance workload is little, but also makes to run more secure, reliable；
(4) technical process and equipment are all very simple, and low temperature spiral-flow type supersonic speed isolation technics is a kind of refrigeration of innovation, takes off
The de- hydrocarbon high efficiency technical of water, integrates the functions such as refrigeration, gas-liquid separation, disposable generation dry gas, is applied to Gas-treating processes
Flow process, it is possible to reduce equipment, the short route of real meaning is realized, so as to cost of reducing investment outlay；
(5) itself no consumption, therefore operating cost is low；
(6) in running, noise is little, without discharge, pollution-free, on environment without impact, practicable full friendly process；
(7) small volume, therefore equipment takes up an area and to occupy space little；
(8) different cyclones and diffuser can be configured according to different purposes configuration supersonic speed and subsonic jet pipe, with
Different needs are adapted to, or even punching withdrawal liquid can also be carried out on active section wall as needed.
Description of the drawings
Fig. 1 is NGsd apparatus structure schematic diagrams, wherein, 1- gas accesses；2- impeller inducer cyclones；3- supersonic speed daraf(reciprocals of farad)
That jet pipe；4- outer tubes；5- separates back taper；6- diffusers；7- liquid outlets；Gas vent after 8- separation.
Fig. 2 is embodiment gas dehydration hydrocarbon removal process process chart.
Specific embodiment
The present invention is dynamic with reference to gas using the low temperature spiral-flow type supersonic speed separator obtained by inventor's Jing creative works
Mechanics, thermodynamics and hydromechanical theory, through adiabatic expansion low temperature Supersonic Flow is formed, and separates Jing using eddy flow field exhausted
Cryogenic condensation moisture content and heavy hydrocarbon component that thermal expansion is formed.Effectively solving is reduced in exploration and development and oil gas field production process and is set
Standby floor space, mitigates basis and bears a heavy burden, and cost efficiency is processed containing the urgent of the high acid gas such as high-hydrogen sulfide, carbon dioxide
Demand.
The invention provides low temperature spiral-flow type supersonic speed separator, the device includes gas access 1, impeller inducer eddy flow
Gas vent 8 is constituted after device 2, supersonic speed Rafael nozzle 3, outer tube 4, separation back taper 5, diffuser 6, liquid outlet 7, separation.
Further, in above-mentioned NGsd devices, the supersonic speed De Laval noz(zle) is divided into four parts：Stable section, subsonic speed
Contraction section, throat, supersonic speed expansion segment.
Effect of the low temperature spiral-flow type supersonic speed separator in natural gas liquefaction flow process and traditional liquefaction process
Decompressor and J-T valves quite, be typically more suitable for bleed pressure it is higher in the case of partial liquefaction technique.Natural gas is into low
Need first to carry out precooling before warm spiral-flow type supersonic speed separator.Using the low temperature spiral-flow type supersonic speed separation removal device,
(hypothesis can work with liquid, and isentropic efficiency is that 75%) gas deliquescence process is counted for J-T valves and the decompressor of hypothesis
Calculate and compare.When precooling temperature is -80 DEG C, low temperature spiral-flow type supersonic speed separator, J-T valves are respectively adopted under different pressures
And the comparison of computational results of the liquefaction process of decompressor.There it can be seen that in the case where inlet pressure is very high, low temperature
The advantage of spiral-flow type supersonic speed separator is not obvious, not only liquefaction efficiency less than 75% efficiency decompressor, and with J-T valves
Difference is also less and less, but no matter under any circumstance its liquefaction efficiency is above J-T valves.In the case where pressure is relatively low, adopt
With J-T valves now oneself cannot obtain LNG liquid, and then liquefied fraction even above expands to adopt low temperature spiral-flow type supersonic speed separator
Machine (75% isentropic efficiency, it is assumed that can work under band liquid), and movement-less part, thus it is now super using low temperature spiral-flow type
It is particularly evident that velocity of sound separates separator advantage.
Second technical problem to be solved by this invention is to provide gas dehydration hydrocarbon removal process, the technique include with
Lower step：
(1), natural gas _ raw material gas into NGsd devices, and revolve in NGsd devices Jing after heat exchanger cooling through high speed
Flow, step-down, the gas-liquid mixture of cooling and speedup, isolated water and lighter hydrocarbons, dry gas, shunting dry gas are expanded in jet pipe；
(2) water and the gas-liquid mixture of lighter hydrocarbons, shunting dry gas that, step (1) is obtained enters gas-liquid separator, isolated
Water and lighter hydrocarbons, shunting dry gas.
(3) the shunting dry gas that the dry gas and step (2) that, step (1) is obtained is obtained, Jing gas mixers mixing, is recycled into
It is outer defeated after heat exchanger, with natural gas _ raw material gas heat exchange.
Specifically, in above-mentioned gas dehydration hydrocarbon removal process, natural gas _ raw material gas initially enter cyclone rotation, produce and add
Speed is l × 106m/s2Eddy flow, the eddy flow produces one or more gases in the tangential direction of supersonic nozzle inlet surface
Jet, and expansion step-down, cooling and speedup in jet pipe.Because natural gas temperature is reduced, vapor therein and NGL are condensed into
Drop, " is got rid of " on tube wall, so as to realize gas-liquid separation in the presence of the tangential velocity and centrifugal force that rotation is produced.Due to
In latter half of deceleration, supercharging, the thermogenic action through diffuser of jet pipe, the pressure energy of natural gas Jing NGsd device nozzle loss is big
Part is recovered, so as to greatly reduce the pressure loss of natural gas.Due to natural gas it is latter half of to diffuser in jet pipe
Pressure go up, make the inlet outlet pressure differential of NGsd appliance arrangements much smaller than the pressure reduction of supersonic nozzle.Therefore, with traditional fore-telling T valves
Compare with expander refrigeration equipment, in the case of same pressure differential, NGsd devices can make natural gas produce bigger temperature drop.Although
NGsd devices can make natural gas produce bigger temperature drop, and while deviate from water and NGL, but because gas flow is in NGsd
Flowing velocity can exceed 550m/s, the time of staying is very short, therefore, gas hydrates will not be generated inside NGsd.
Specifically, in above-mentioned steps (1), natural gas _ raw material gas enter NGsd devices, by adjusting the rotation of entrance guiding impeller
The anglec of rotation of stream device blade, makes charge raw material gas, forms strong eddy flow field, and generation tangential acceleration is l × 106m/s2's
Eddy flow, the eddy flow produces one or more gas jets in the tangential direction of supersonic nozzle inlet surface.
Specifically, in above-mentioned steps (1), natural gas _ raw material gas Jing after entrance guiding impeller cyclone, obtain 20 DEG C of temperature,
The saturated natural gas of pressure 10MPa, saturated natural gas by supersonic speed De Laval noz(zle), Mach number Ma >=l its temperature and pressure
To reduce, form low-temp low-pressure, the heavy hydrocarbon and water vapour in natural gas will reach hypersaturated state and start to condense, and nucleation occur and shows
As, and drop starts growth, forms gas-liquid mixture.Then, produce in straight pipeline after gas-liquid mixture is by being placed in jet pipe
The empennage of eddy flow, forms strong eddy flow field, in flowing drop under the influence of centrifugal force eddy flow at tube wall.
Specifically, the drop drop for obtaining in above-mentioned supersonic speed De Laval noz(zle) is thrown to one-level by centrifugal action to be expanded
The tube wall of scattered section, thus liquid flows along tube wall, and the gas at tube wall will be comprising part heavy hydrocarbon and moisture composition, Jing outlets
Discharge.Dry gas occupy main flow center, and by back taper centre bore back taper portion straight length is entered, and in back taper straight length, carries out current stabilization liter
Pressure.In two grades of diffusers, through one weak impact ripple, the dry gas of generation then flows into diffuser pipe, and speed is converted into pressure, gas
Flowing pressure returns to the 70～80% of inlet pressure.
Finally it should be noted that：Below only to illustrate technical scheme, rather than a limitation；Although with reference to front
State each embodiment to be described in detail the present invention, it will be understood by those within the art that：It still can be right
Technical scheme described in foregoing embodiments is modified, and is either carried out equivalent to which part or all technical characteristic and is replaced
Change；And these modifications or replacement, do not make the scope of the essence disengaging technical solution of the present invention of appropriate technical solution.
Claims (8)
1. low temperature spiral-flow type supersonic speed separator, it is characterised in that the device include gas access, impeller inducer cyclone,
Gas vent composition after supersonic speed Rafael nozzle, separation back taper, boosting diffuser, liquid outlet, separation.
2. low temperature spiral-flow type supersonic speed separator according to claim 1, it is characterised in that the supersonic speed Laval spray
Pipe is divided into four parts：Stable section, subsonic speed contraction section, throat, supersonic speed expansion segment.
3. gas dehydration hydrocarbon removal process, it is characterised in that the technique is comprised the following steps：
(1), natural gas _ raw material gas Jing heat exchanger cooling after, into NGsd devices, and in NGsd devices through high-speed rotational,
Gas-liquid mixture, the dry gas of expansion step-down, cooling and speedup, isolated water and lighter hydrocarbons in jet pipe；
(2) water and the gas-liquid mixture of lighter hydrocarbons that, step (1) obtains enters gas-liquid separator, isolated water and lighter hydrocarbons,
Shunting dry gas.
4. gas dehydration hydrocarbon removal process according to claim 3, it is characterised in that the technique also includes step (3)：It is described
The shunting dry gas that the dry gas and step (2) that step (1) is obtained is obtained, Jing gas mixers mixing, is recycled into the heat exchanger, with
It is outer defeated after natural gas _ raw material gas heat exchange, obtain dry gas product.
5. gas dehydration hydrocarbon removal process according to claim 3, it is characterised in that in step (1), the gas material
Temperature of the gas Jing after heat exchanger cooling is -80 DEG C.
6. gas dehydration hydrocarbon removal process according to claim 3, it is characterised in that in step (1), the high-speed rotational is produced
Raw tangential acceleration is l × 106m/s2Eddy flow.
7. gas dehydration hydrocarbon removal process according to claim 3, it is characterised in that in step (1), the raw natural gas
20 DEG C of temperature, the saturated natural gas of pressure 10MPa are produced Jing after high-speed rotational.
8. gas dehydration hydrocarbon removal process according to claim 3, it is characterised in that in step (1), the speed after the speedup
Degree ＞ 550m/s.
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