CN106433832A - Process and device for removing CO2 in natural gas - Google Patents
Process and device for removing CO2 in natural gas Download PDFInfo
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- CN106433832A CN106433832A CN201610894242.9A CN201610894242A CN106433832A CN 106433832 A CN106433832 A CN 106433832A CN 201610894242 A CN201610894242 A CN 201610894242A CN 106433832 A CN106433832 A CN 106433832A
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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
-
- 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
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/103—Sulfur containing contaminants
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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
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
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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
-
- 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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
-
- 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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
- C10L2290/541—Absorption of impurities during preparation or upgrading of a fuel
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- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention provides a process and a device for removing CO2 in natural gas. The process comprises steps as follows: the natural gas as a raw material after subjected to cyclone separation enters an absorption tower and is subjected to CO2 removing, purified gas after CO2 removing is discharged from the top of the absorption tower, a rich solution at the bottom of the adsorption tower is sequentially subjected to high-pressure flash evaporation, medium-pressure flash evaporation and low-pressure flash evaporation, high-pressure flashing steam, medium-pressure flashing steam and low-pressure flashing steam are circulated to the feed gas through a high-pressure compressor, a medium-pressure compressor and a low-pressure compressor respectively, a flashing solution is subjected to normal-pressure desorption and vacuum desorption to desorb CO2, meanwhile, H2S and H2O are desorbed, and a vacuum desorption solution enters the top of the adsorption tower to be recycled. The method has the advantages of being simple in process, low in energy consumption, high in CO2 removing rate and high in hydrocarbon recovery rate, and can remove a small amount of H2S and part of water in the natural gas simultaneously, and purpose of natural gas purification is achieved.
Description
Technical field
The invention belongs to natural gas processing field, especially relate to CO in a kind of removing natural gas2Technique and device.
Background technology
Natural gas is the gaseous hydrocarbons extraction material of oil, is high-grade fuel and industrial chemicals.In natural gas, methane accounts for absolutely
Great majority, separately have a small amount of ethane, propane and butane, typically also contain hydrogen sulfide, carbon dioxide, aqueous vapor etc. in addition.Natural gas
In carbon dioxide be common corrosive medium during oil field produces, be also the key factor of natural-gas transfer pipeline corrosion.Corrosion
The faults such as fracture, the feed-line explosion of natural gas well set can be caused.Corrode the leakage causing to be likely to cause fire incident, give
The safe operation of gas pipeline threatens.Additionally, the too high calorific value that also can reduce natural gas of carbon dioxide content, being allowed to cannot
Meet the requirement of the technical indicator defined of Chinese commodity natural gas.Therefore, it is necessary to by the carbon dioxide being rich in natural gas
Effectively removed.
Existing natural gas decarburization technique mainly includes solvent absorption, membrane separation process, membranes, cryogenic fractionation, pressure swing adsorption method
Etc. several big class.Solvent absorption can be further subdivided into hydramine method, hot potash method, physical solvent process etc. again.Hydramine method and hot potassium
Alkaline process is using solvent and CO2Method chemical reaction occurring and realizing decarburization.Hydramine method is concentrated mainly on complex solvent component
Selection and improve on.But hydramine method flow process is more complicated, equipment corrosion is serious, and solution internal circulating load is big, high energy consumption, and carbon dioxide is inhaled
Fruit of producing effects is undesirable.The equipment corrosion problem of hot potash method is also more serious, and energy consumption is also higher.Physical solvent process is to utilize CO2?
Dissolved in absorbent and realized remove method, the method due to there being a certain amount of hydrocarbon loss, for natural gas decarbonization
The heavy hydrocarbon in natural gas should first be sloughed before.
Content of the invention
It is an object of the invention to provide the natural gas decarbonization work that a kind of flow process is simple, energy consumption is low, carbon dioxide eliminating rate is high
Skill, this technique belongs to physical solvent process.This technique is not required to heat, and only needs electric energy and a small amount of cooling water, total energy consumption is low, operating cost
Low, also can remove a small amount of hydrogen sulfide and water, products C O simultaneously2Gas purity is higher, and can improve the rate of recovery of hydro carbons.
The process step of the invention is：Containing CO2Raw natural gas carry out cyclonic separation first, isolate free water,
Heavy hydrocarbon and solid particle, the absorbent that cyclonic separation natural gas out is entered absorption tower bottom and entered with absorption tower teeming contacts,
Carry out CO under 3.0-12.0MPa2Removing, de- CO2Purified gas self-absorption tower top afterwards is discharged, purified gas CO2Content can be controlled in
In the range of 0.5%-3%, absorption tower bottom rich solution carries out high pressure flash, and high pressure flash pressure is 2.0-4.0MPa, and high pressure flash goes out
Gas be recycled in unstripped gas through recycle compressor, the liquid that high pressure flash goes out carries out middle pressure flash distillation, middle pressure flashing pressure again
For 1.0-2.0MPa, the gas that middle pressure flashes off is recycled in unstripped gas through recycle compressor, and the liquid that middle pressure flashes off enters again
Row low pressure flash, low pressure flash pressure is 0.2-1.0MPa, and the gas that low pressure flash goes out is recycled to unstripped gas through recycle compressor
In, the liquid that low pressure flash goes out goes normal pressure to parse, and parses CO2、H2S、H2O and heavy hydrocarbon, normal pressure desorbed solution carries out Vacuum solutions again
Analysis, parses CO further2、H2S、H2O and heavy hydrocarbon, vacuum analysis liquid, as cyclic absorption agent, boosts to through solvent circulating pump
3.4-12.4MPa going to absorb tower top circulation.
In above-mentioned technique, the gas that high pressure flash goes out can be recycled in unstripped gas through high pressure compressor, and middle pressure flashes off
Gas be recycled in unstripped gas through intermediate pressure compressor, the gas that low pressure flash goes out is recycled in unstripped gas through low pressure compressor.
Gas alternatively, it is also possible to discharge low pressure compressor enters intermediate pressure compressor after merging with middle pressure flashed vapour, then by middle pressure
The gas that compressor is discharged and high pressure flash gas are combined into high pressure compressor, finally compress Posterior circle together to unstripped gas.
The circulation compression set of the present invention can largely concentrate the carbon dioxide in absorption tower when reclaiming natural gas, beneficial to suction
Receive.
In order to make full use of system capacity, absorption tower bottom rich solution can dodge through the laggard horizontal high voltage of high pressure hydraulic turbine step-down
Steam, the power of high pressure hydraulic turbine is available to solvent circulating pump；During the liquid that high pressure flash goes out passes through, pressure hydraulic turbine is depressured
After carry out middle pressure flash distillation, the power of middle pressure hydraulic turbine is supplied to solvent circulating pump.
The absorbent that the technique of the present invention adopts is propene carbonate (PC) or propene carbonate is sweet with two mustard acyl phosphatidyls
The combination of oily (DEPG), CO in raw natural gas2Partial pressure >=0.5MPa, C3Above heavy hydrocarbons content≤2%, to reduce heavy hydrocarbon damage
Lose.
The invention still further relates to CO in a kind of removing natural gas2Device, as shown in figure 1, include cyclone separator 1, absorb
Tower 2, high pressure flash tower 3, middle pressure flash column 4, Low Pressure Flashing Column 5, normal pressure Analytic Tower 6, vacuum analysis tower 7, circulating pump 10, vacuum
Pump 11, circulation compression set 12, raw natural gas air inlet pipeline S0 is connected with cyclone separator 1, and the natural gas of initial gross separation goes out
The two ends of mouth pipeline S1 are located at cyclone separator 1 top and absorption tower 2 bottom respectively, and purified natural gas discharge line S12 is located at
Absorption tower 2 top, absorption tower rich solution discharge line S2 arranges high pressure hydraulic turbine 8, and the two ends of S2 are located at absorption tower 2 bottom respectively
Portion and high pressure flash tower 3 top, press hydraulic turbine 9 during high pressure flash liquid discharge line S3 is arranged, the two ends of S3 are located at respectively
High pressure flash tower 3 bottom and middle pressure flash column 4 top, the two ends of high pressure flash gas discharge line S101 connect high pressure flash respectively
Tower 3 top and circulation compression set 12, the two ends of middle pressure flash liquid discharge line S4 are located at middle flash column 4 bottom and low of pressing respectively
Pressure flash column 5 top, during the two ends of middle pressure flashed vapour discharge line S102 connect respectively, dress is compressed with circulation in pressure flash column 4 top
Put 12, the two ends of low pressure flash liquid discharge line S5 are located at Low Pressure Flashing Column 5 bottom and normal pressure Analytic Tower 6 top, low pressure respectively
The two ends of flashed vapour discharge line S103 connect Low Pressure Flashing Column 5 top and circulation compression set 12 respectively, circulate compression set
Outlet pipe S11 is communicated with raw natural gas air inlet pipeline S0, and normal pressure resolution gas discharge line S8 is located at normal pressure and parses top of tower,
The two ends of normal pressure desorbed solution discharge line S6 connect normal pressure Analytic Tower 6 bottom and vacuum analysis tower 7 top, Vacuum solutions gassing respectively
Vavuum pump 11 is provided with discharge line S9, S9 is located at vacuum analysis tower 7 top, S8 and S9 converge after as gas exhaust piping, very
Solvent circulating pump 10 is provided with empty desorbed solution discharge line S7, the two ends of S7 connect vacuum analysis tower 7 bottom and absorption respectively
Tower 2 top.
Described circulation compression set 12 is by high pressure compressor 121, intermediate pressure compressor 122 and 123 groups of low pressure compressor
The compressor bank becoming, high pressure flash gas discharge line S101 is connected with high pressure compressor 121, middle pressure flashed vapour discharge line S102
It is connected with intermediate pressure compressor 122, low pressure flash gas discharge line S103 is connected with low pressure compressor 123, high pressure compressor 121
The outlet pipe S113 of outlet pipe S111, the outlet pipe S112 of intermediate pressure compressor 122 and low pressure compressor 123 and raw material
Natural gas air inlet pipe road S0 connects.
Additionally, the pipeline of described high, medium and low voltage compressor can also be arranged as Fig. 2：Low pressure compressor discharge line S113
Connect with middle pressure flashed vapour discharge line S102, intermediate pressure compressor discharge line S112 and high pressure flash gas discharge line S101 phase
Connect, high pressure compressor discharge line S111 is connected with pipeline S11.
Assembly of the invention utilizes high pressure hydraulic turbine 8, middle pressure hydraulic turbine 9 to be depressured the energy of simultaneously recovery system to rich solution
Amount, wherein high pressure hydraulic turbine 8 is arranged on the rich solution discharge line S2 of absorption tower, and middle pressure hydraulic turbine 9 is arranged on high pressure flash
On liquid discharge line S3.
The present invention has the advantages and positive effects that：1st, energy consumption is low, and the present invention only needs consuming electric power, and compressor outlet is natural
Gas Cooler can adopt air cooler, or the method using water cooler after first air cooler, and seldom, process energy consumption is far below cooling water inflow
EMDEA process energy consumption；2nd, absorbent regeneration, only with flash distillation, is not required to heat, needs thermal regeneration unlike other techniques；3、
Products C O2Gas purity is higher, and flammable gas component is few, in heavy hydrocarbon and H2When S content is high, products C O2Purity may be up to 97%
More than；4th, the purified natural gas rate of recovery is high, and product loss is few；5th, the water dew point in saturated natural gas, follow-up sky can be reduced simultaneously
So gas hydrocarbon dew point controls can meet the requirement of gas dehydration TEG device without adding dehydration device simultaneously；6th, few in purified gas
The H2S of amount can be absorbed simultaneously, absorptivity about 95%.
Brief description
Fig. 1 is assembly of the invention schematic diagram
Fig. 2 is the schematic diagram that apparatus of the present invention adopt during second compressor bank
In figure：
Equipment：
1st, cyclone separator 2, absorption tower 3, high pressure flash tower
4th, middle pressure flash column 5, Low Pressure Flashing Column 6, normal pressure Analytic Tower
7th, vacuum analysis tower 8, high pressure hydraulic turbine 9, middle pressure hydraulic turbine
10th, circulating pump 11, vavuum pump 12, circulation compression set
121st, high pressure compressor 122, intermediate pressure compressor 123, low pressure compressor
Pipeline：
S0, raw natural gas air inlet pipeline
S1, the gas outlet pipeline of initial gross separation
S2, absorption tower rich solution discharge line
S3, high pressure flash liquid discharge line
S4, middle pressure flash liquid discharge line
S5, low pressure flash liquid discharge line
S6, normal pressure desorbed solution discharge line
S7, vacuum analysis liquid discharge line
S8, normal pressure resolution gas discharge line
S9, Vacuum solutions gassing discharge line
S101, high pressure flash gas discharge line
S102, middle pressure flashed vapour discharge line
S103, low pressure flash gas discharge line
S11, circulation compression set outlet pipe
S111, high pressure compressor outlet pipe
S112, intermediate pressure compressor outlet pipe
S113, low pressure compressor outlet pipe
S12, purified natural gas discharge line
Specific embodiment
Raw natural gas treating capacity：100×104m3/ d (20 DEG C, 101.325kPa)
Raw natural gas component：
Processing step is as shown in Figure 2：10MPa, 35 DEG C containing CO2Raw natural gas initially enter cyclone separator 1, point
Separate out free water, heavy hydrocarbon and solid particle；S1 enters absorption tower 2 bottom simultaneously to cyclone separator 1 natural gas out by the road
The absorbent propene carbonate being entered with absorption tower teeming is contacted, and carries out de- CO under 9.9MPa pressure2, de- CO2Purified gas afterwards are certainly
Absorption tower top manifold S12 discharges；Absorption tower bottom rich solution enters high pressure flash tower through pipeline S2 after high pressure hydraulic turbine 8 step-down
3 carry out high pressure flash, and high pressure flash pressure is 4.0MPa, and S101 enters high pressure compressor to the gas that high pressure flash goes out by the road
121 are recycled in unstripped gas, and during the liquid that high pressure flash goes out enters through pipeline S3 after middle pressure hydraulic turbine 9 step-down, pressure is dodged
Steam tower 4 and carry out middle pressure flash distillation, middle pressure flashing pressure is 1.5MPa, pressure compression in the gas that middle pressure flashes off S102 entrance by the road
Machine 122 is recycled in unstripped gas, enters Low Pressure Flashing Column 5 through pipeline S4 and carry out low pressure sudden strain of a muscle after the liquid step-down that middle pressure flashes off
Steam, low pressure flash pressure is 0.5MPa, the gas that low pressure flash the goes out low pressure compressor 123 of S103 entrance by the road is recycled to raw material
In gas, S5 removes normal pressure Analytic Tower 6 to the liquid that low pressure flash goes out by the road, parses CO2、H2S、H2O and a small amount of heavy hydrocarbon by the road
S8 discharges, and S6 enters vacuum analysis tower 7 to normal pressure desorbed solution by the road, parses CO further2、H2S、H2O and a small amount of heavy hydrocarbon warp
Pipeline S9 discharges, and as cyclic absorption agent, S7 goes to inhale vacuum analysis liquid by the road to boost to 10.4MPa through solvent circulating pump 10
Receive tower top circulation.
The C1 rate of recovery is 99.88%, the C2 rate of recovery is 80%；
CO in purified gas2Content 1.42%；
H in purified gas2O is 0%, and after device, the natural gas of saturation is changed into very dry natural gas, follow-up natural gas
Hydrocarbon dew point control can without plus dehydration device；
Products C O2The purity of gas is 95.4%；
Products C O2Tolerance be：9.88x104m3/ d (20 DEG C, 101.325kPa)；
Purified natural gas：90.1x104m3/ d (20 DEG C, 101.325kPa)；
H2The yield of S is 98%.
The foregoing describe the preferred embodiments of the invention, it will be appreciated by those of skill in the art that this is only to lift
Example explanation, protection scope of the present invention is defined by the appended claims.Those skilled in the art is without departing substantially from this
On the premise of bright principle and essence, various changes or modifications can be made to these embodiments, but these changes and modification
Each fall within protection scope of the present invention.
Claims (10)
1. CO in a kind of removing natural gas2Technique it is characterised in that：Containing CO2Raw natural gas carry out cyclonic separation first,
Isolate free water, heavy hydrocarbon and solid particle, cyclonic separation natural gas out enter absorption tower bottom and with absorption tower teeming
The absorbent contact entering, carries out CO2Removing, de- CO2Purified gas self-absorption tower top afterwards is discharged, and absorption tower bottom rich solution enters horizontal high voltage
Flash distillation, the gas that high pressure flash goes out is recycled in unstripped gas through recycle compressor, and the liquid that high pressure flash goes out carries out middle pressure flash distillation,
The gas that middle pressure flashes off is recycled in unstripped gas through recycle compressor, and the liquid that middle pressure flashes off carries out low pressure flash, low pressure
The gas flashing off is recycled in unstripped gas through recycle compressor, and the liquid that low pressure flash goes out goes normal pressure to parse, and parses CO2、
H2S、H2O and a small amount of heavy hydrocarbon, normal pressure desorbed solution carries out vacuum analysis again, parses CO further2、H2S、H2O and a small amount of weight
Hydrocarbon, vacuum analysis liquid, as cyclic absorption agent, goes to absorb tower top circulation through solvent circulating pump boosting.
2. CO in removing natural gas according to claim 12Technique it is characterised in that：CO in raw natural gas2Point
Pressure >=0.5Mpa, C3Above heavy hydrocarbons content≤2%, absorption pressure tower is 3.0-12.0MPa, and high pressure flash pressure is 2.0-
4.0MPa, middle pressure flashing pressure is 1.0-2.0MPa, and low pressure flash pressure is 0.2-1.0MPa, and vacuum analysis liquid follows through solvent
Ring pump boosts to 3.4-12.4MPa.
3. CO in removing natural gas according to claim 12Technique it is characterised in that：The gas that high pressure flash goes out is through height
To unstripped gas, the gas that middle pressure flashes off is recycled in unstripped gas pressure compressor cycle through intermediate pressure compressor, and low pressure flash goes out
Gas be recycled in unstripped gas through low pressure compressor.
4. CO in removing natural gas according to claim 12Technique it is characterised in that：The gas that low pressure compressor is discharged
Intermediate pressure compressor is entered, the gas that intermediate pressure compressor is discharged enters high after merging with high pressure flash gas after merging with middle pressure flashed vapour
Pressure compressor, through in high pressure compressed Posterior circle to unstripped gas.
5. CO in removing natural gas according to claim 12Technique it is characterised in that：Absorption tower bottom rich solution is through high pressure
Hydraulic turbine is depressured laggard horizontal high voltage flash distillation, and the power of high pressure hydraulic turbine is supplied to solvent circulating pump, the liquid that high pressure flash goes out
Body carries out middle pressure flash distillation after middle pressure hydraulic turbine step-down, and the power of middle pressure hydraulic turbine is supplied to solvent circulating pump.
6. CO in removing natural gas according to claim 12Technique it is characterised in that：Absorbent is propene carbonate
Or the combining of propene carbonate and two mustard acyl phosphatidyl glycerol (DEPG) (PC).
7. CO in a kind of removing natural gas2Device it is characterised in that：Dodge including cyclone separator (1), absorption tower (2), high pressure
Steam tower (3), middle pressure flash column (4), Low Pressure Flashing Column (5), normal pressure Analytic Tower (6), vacuum analysis tower (7), circulating pump (10), true
Empty pump (11), circulation compression set (12), raw natural gas air inlet pipeline (S0) is connected with cyclone separator (1), initial gross separation
Gas outlet pipeline (S1) two ends respectively be located at cyclone separator (1) top and absorption tower (2) bottom, purified natural gas
Discharge line (S12) is located at absorption tower (2) top, and absorption tower rich solution discharge line (S2) is upper to arrange high pressure hydraulic turbine (8),
(S2) two ends are located at absorption tower (2) bottom and high pressure flash tower (3) top respectively, and high pressure flash liquid discharge line (S3) sets
Put middle pressure hydraulic turbine (9), the two ends of (S3) are located at high pressure flash tower (3) bottom and middle pressure flash column (4) top, high pressure respectively
The two ends of flashed vapour discharge line (S101) connect high pressure flash tower (3) top and circulation compression set (12) respectively, and middle pressure is dodged
The two ends of steaming liquid discharge line (S4) are located at middle pressure flash column (4) bottom and Low Pressure Flashing Column (5) top, middle pressure flashed vapour respectively
Flash column (4) top and circulation compression set (12) are pressed in the two ends of discharge line (S102) in connecting respectively, low pressure flash liquid is arranged
The two ends going out pipeline (S5) are located at Low Pressure Flashing Column (5) bottom and normal pressure Analytic Tower (6) top, low pressure flash gas discharge pipe respectively
The two ends on road (S103) connect Low Pressure Flashing Column (5) top and circulation compression set (12) respectively, circulate compression set escape pipe
Road (S11) is communicated with raw natural gas air inlet pipeline (S0), and normal pressure resolution gas discharge line (S8) is located at normal pressure and parses top of tower,
The two ends of normal pressure desorbed solution discharge line (S6) connect normal pressure Analytic Tower (6) bottom and vacuum analysis tower (7) top, vacuum respectively
Vavuum pump (11) is provided with resolution gas discharge line (S9), (S9) is located at vacuum analysis tower (7) top, and (S8) and (S9) converges
Afterwards as gas exhaust piping, vacuum analysis liquid discharge line (S7) are provided with solvent circulating pump (10), the two ends of (S7) connect respectively
Connect vacuum analysis tower (7) bottom and absorption tower (2) top.
8. CO in removing natural gas according to claim 72Device it is characterised in that：Circulation compression set (12) be by
The compressor bank that high pressure compressor (121), intermediate pressure compressor (122) and low pressure compressor (123) form, high pressure flash gas is arranged
Go out pipeline (S101) to be connected with high pressure compressor (121), middle pressure flashed vapour discharge line (S102) and intermediate pressure compressor (122) phase
Even, low pressure flash gas discharge line (S103) is connected with low pressure compressor (123), the outlet pipe of high pressure compressor (121)
(S111), the outlet pipe (S112) of intermediate pressure compressor (122) and the outlet pipe (S113) of low pressure compressor (123) with former
Material natural gas air inlet pipe road (S0) connects.
9. CO in removing natural gas according to claim 72Device it is characterised in that：Low pressure compressor discharge line
(S113) connect with middle pressure flashed vapour discharge line (S102), intermediate pressure compressor discharge line (S112) is discharged with high pressure flash gas
Pipeline (S101) connects, and high pressure compressor discharge line (S111) is connected with pipeline (S11).
10. CO in removing natural gas according to claim 72Device it is characterised in that：Also include high pressure hydraulic turbine
(8), middle pressure hydraulic turbine (9), wherein high pressure hydraulic turbine (8) is arranged on absorption tower rich solution discharge line (S2), middle hydraulic fluid
Power turbine (9) is arranged on high pressure flash liquid discharge line (S3).
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| CN201610894242.9A CN106433832A (en) | 2016-10-14 | 2016-10-14 | Process and device for removing CO2 in natural gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610894242.9A CN106433832A (en) | 2016-10-14 | 2016-10-14 | Process and device for removing CO2 in natural gas |
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| CN201610894242.9A Pending CN106433832A (en) | 2016-10-14 | 2016-10-14 | Process and device for removing CO2 in natural gas |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107098788A (en) * | 2017-06-06 | 2017-08-29 | 中国石油集团工程设计有限责任公司 | A kind of device and method that ethane carbon dioxide removal is reclaimed in pipe natural gas |
| CN108744888A (en) * | 2018-06-13 | 2018-11-06 | 中国石油大学(华东) | A kind of carbon dioxide recovery system, in accordance suitable for offshore platform oil-gas mining tail gas |
| CN110066695A (en) * | 2019-04-30 | 2019-07-30 | 李育 | Natural gas nitrogen rejection facility and method |
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