CN108641765A - Remove the process system and method for carbon dioxide in natural - Google Patents
Remove the process system and method for carbon dioxide in natural Download PDFInfo
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- CN108641765A CN108641765A CN201810670712.2A CN201810670712A CN108641765A CN 108641765 A CN108641765 A CN 108641765A CN 201810670712 A CN201810670712 A CN 201810670712A CN 108641765 A CN108641765 A CN 108641765A
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 148
- 238000000034 method Methods 0.000 title claims abstract description 90
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 74
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 74
- 230000008569 process Effects 0.000 title claims abstract description 47
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 140
- 238000001179 sorption measurement Methods 0.000 claims abstract description 127
- 239000007789 gas Substances 0.000 claims abstract description 108
- 239000003345 natural gas Substances 0.000 claims abstract description 69
- 238000007664 blowing Methods 0.000 claims abstract description 41
- 230000008929 regeneration Effects 0.000 claims description 35
- 238000011069 regeneration method Methods 0.000 claims description 35
- 238000010438 heat treatment Methods 0.000 claims description 33
- 230000009102 absorption Effects 0.000 claims description 19
- 238000010521 absorption reaction Methods 0.000 claims description 19
- 239000000446 fuel Substances 0.000 claims description 16
- 239000002808 molecular sieve Substances 0.000 claims description 16
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 16
- 239000002737 fuel gas Substances 0.000 claims description 13
- 238000001816 cooling Methods 0.000 claims description 11
- 239000002994 raw material Substances 0.000 claims description 11
- 238000003860 storage Methods 0.000 claims description 11
- 239000004215 Carbon black (E152) Substances 0.000 claims description 9
- 229930195733 hydrocarbon Natural products 0.000 claims description 9
- 150000002430 hydrocarbons Chemical class 0.000 claims description 9
- 239000012535 impurity Substances 0.000 claims description 9
- 238000000746 purification Methods 0.000 claims description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- 230000008676 import Effects 0.000 claims description 8
- 239000013589 supplement Substances 0.000 claims description 7
- 239000000945 filler Substances 0.000 claims description 5
- 239000003463 adsorbent Substances 0.000 claims description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 3
- 230000008859 change Effects 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 239000000741 silica gel Substances 0.000 claims description 3
- 229910002027 silica gel Inorganic materials 0.000 claims description 3
- 230000009469 supplementation Effects 0.000 claims description 3
- 238000006073 displacement reaction Methods 0.000 claims description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims 1
- ZZVUWRFHKOJYTH-UHFFFAOYSA-N diphenhydramine Chemical compound C=1C=CC=CC=1C(OCCN(C)C)C1=CC=CC=C1 ZZVUWRFHKOJYTH-UHFFFAOYSA-N 0.000 abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 6
- 231100000331 toxic Toxicity 0.000 abstract description 3
- 230000002588 toxic effect Effects 0.000 abstract description 3
- 239000003153 chemical reaction reagent Substances 0.000 abstract description 2
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 description 6
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 description 6
- 230000000274 adsorptive effect Effects 0.000 description 3
- 230000018044 dehydration Effects 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 208000019901 Anxiety disease Diseases 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 230000036506 anxiety Effects 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000005262 decarbonization Methods 0.000 description 2
- 238000005261 decarburization Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
- 239000012190 activator Substances 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
Classifications
-
- 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
-
- 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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0462—Temperature swing adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
- B01D2256/245—Methane
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/403—Further details for adsorption processes and devices using three beds
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
Remove the process system and method for carbon dioxide in natural.Traditional wet method removes carbon dioxide in natural, and flow is complicated, and equipment is various, and hydramine reagent is toxic, and make-up solution and desalted water are needed in operation.The present invention forms：Raw natural gas entrance, it is characterized in that：Raw natural gas entrance by valve respectively with adsorption tower A（1）, adsorption tower B（2）, adsorption tower C（3）Inlet tube connection, adsorption tower A, adsorption tower B, adsorption tower C outlet connect with purified natural gas pipe by valve, purified natural gas pipe is connected by valve with each cold blowing inlet tube, each cold blowing outlet and cold blowing Gas Cooler（7）Inlet tube is connected, and cold blowing Gas Cooler outlet is connected with purified natural gas pipe, heater（5）Outlet is connected with adsorption tower A, adsorption tower B, adsorption tower C inlet tubes respectively by valve, and circularly-supercharged machine outlet is connected with heater inlet pipe.The present invention is used to remove the process system of carbon dioxide in natural.
Description
Technical field：
The present invention relates to the natural gas preconditioning technique fields in liquefaction Technology of Natural Gas, and in particular in a kind of removing natural gas
The process system and method for carbon dioxide.
Background technology：
Natural gas is a kind of environmentally protective, economical and practical, safe and reliable high-grade energy, develops gas industry, natural gas liquid
The research of gas purifying process is also particularly important in change technology, because in natural gas relatively high-solidification point component such as carbon dioxide,
Moisture and heavy hydrocarbon etc. can be solidified in gas deliquescence process and occluding device, it is necessary to be removed before liquefaction；Traditional
Wet method removes carbon dioxide in natural, and flow is complicated, and equipment is various, and hydramine reagent is toxic, and make-up solution is needed in operation
And desalted water.
Natural gas carbon dioxide removal processing method can be divided into two kinds of wet method and dry method, the development of wet method carbon dioxide removal more at
Ripe and application is more for hydramine method, hydramine method have absorb, regenerated technique removing precision is relatively high, treating capacity is big, natural
The advantages that gas methane high income, meets requirement of the LNG devices to purified gas, but hydramine method flow is complicated, and equipment is various, hydramine examination
Agent is toxic, and needs regular replenishment amine liquid and desalted water, carbon dioxide removal process need to be separately positioned with dehydration procedure in operation,
It is bad for the regional applicability of water shortage or land used anxiety；Temp.-change adsorptive process is used in dry method carbon dioxide removal（TSA）It can reach
Natural gas carbon dioxide removal, dehydration and de- heavy hydrocarbon purpose, and pollution, floor space simple, easy to operate, corrosion-free with flow
The small, remarkable advantages such as operating cost is low, but when single utilization routine temp.-change adsorptive process, because carbon dioxide is different from water in regeneration gas
Point and heavy hydrocarbon, can not be separated after cooling, cause this partial regeneration gas that can not recycle, be original with maximum resource utilization
Then, regeneration gas can be used as distributed energy power generation, but in the occasion for not using distributed energy, this partial regeneration gas wastes
Fall, causes the LNG device natural gas methane rate of recovery not high, therefore conventional dry decarburization is not particularly suited for not using distributed energy
The occasion in source.
Invention content：
The object of the present invention is to provide a kind of process system and method for removing carbon dioxide in natural, flow is simple, applicable
Property it is strong, technique use three towers（Also two towers can according to circumstances be used）Temp.-changing adsorption（TSA）It is removed with circularly-supercharged machine serial flow
Carbon dioxide in natural gas or other impurities.
Above-mentioned purpose is realized by following technical scheme：
A kind of process system of removing carbon dioxide in natural, composition include：Raw natural gas entrance, the raw material day
Right gas entrance is connect with the inlet tube of adsorption tower A, adsorption tower B, adsorption tower C respectively by valve, adsorption tower A, adsorption tower B, is inhaled
The outlet of attached tower C is connect by valve with purified natural gas pipe, and purified natural gas pipe passes through valve and each cold blowing inlet tube phase
Even, each cold blowing outlet is connected with cold blowing Gas Cooler inlet tube, and cold blowing Gas Cooler outlet is connected with purified natural gas pipe,
Heater outlet pipe is connected with adsorption tower A, adsorption tower B, adsorption tower C inlet tubes respectively by valve, adsorption tower A, adsorption tower B,
The outlets adsorption tower C stove pipe is connected by valve with storage heater inlet tube, accumulator outlet pipe and circularly-supercharged machine inlet tube
It is connected, circularly-supercharged machine outlet is connected with heater inlet pipe.
The process system of the removing carbon dioxide in natural, the accumulator outlet pipe pass through valve and fuel
Gas surge tank inlet tube connects, and the fuel gas surge tank outlet is connect with fuel gas pipe, and adsorption tower is de- in temperature-rise period
A small amount of mixed gas of the carbon dioxide and natural gas that remove is as fuel.
The process system of the removing carbon dioxide in natural, the accumulator outlet pipe and regeneration Gas Cooler
Inlet tube connects, and the regeneration gas cooler outlet pipe is connect by valve with the raw natural gas pipe, and described follows
Ring supercharger import is arranged purified gas and supplements pipeline.
The process system of the removing carbon dioxide in natural, it is the adsorption tower A, the adsorption tower B, described
Adsorption tower C fillers be that molecular sieve, molecular sieve and activated carbon multiple-hearth, molecular sieve and silica gel multiple-hearth or molecular sieve are inhaled with other
Attached dose of combination, is not limited to other fillers.
A kind of process system and method for removing carbon dioxide in natural, this method comprises the following steps：
First the source of raw natural gas be suitable for various natural gases, be particularly suitable for carbon dioxide in natural gas content compared with
Few situation removes carbon dioxide in natural using two towers or three tower temp.-changing adsorptions with circularly-supercharged machine serial flow；
When using three tower temp.-changing adsorptions with circularly-supercharged machine serial flow, accumulator outlet pipe and regeneration gas cooler inlet pipe
It is connected, regeneration gas cooler outlet pipe is connected by valve with raw natural gas pipe, when adsorption tower A is in adsorbed state, absorption
When tower B is in cold blowing state, adsorption tower C is in heated condition, and circularly-supercharged machine starts adsorption tower C and storage heater, heater
Interior natural gas adsorption closed cycle heating is to prevent adsorption tower C pressure superelevation after heating temperature raising, and portion of natural gas passes through
It is discharged into fuel gas surge tank after storage heater, stops circularly-supercharged machine when closing to an end heating cycle and run and close to be in
The air intake valve of heated condition adsorption tower C；In heated condition adsorption tower C pressure releases to the pressure of a little higher than fuel surge tank, inhale
The boosting of adsorption tower C air intake valves is opened after the gas rich in impurity is largely discharged in attached tower C, this process reduces in adsorption tower
Impurity content in gas；
After adsorption tower C boostings, and circularly-supercharged machine is reruned in a bit of time before system switching, adsorbed
Tower C keeps heated condition, and circularly-supercharged machine import setting cold blowing gas supplements pipeline, net for being used when heating closes to an end
Change gas in gas displacement sorption tower, these gases for containing residual carbon dioxide return to raw material day after regeneration Gas Cooler cooling
Right gas inlet pipeline enters adsorption tower A circulation absorptions；Avoid the carbon dioxide band that residual is excessive in cylinder of next cold blowing stage
To next process；Adsorption tower C initially enters the cold blowing stage adsorption tower B is in adsorbed state simultaneously at the end of heating, and adsorption tower A
In heated condition；It is using Partial cleansing gas that adsorbent in adsorption tower is cooling and cold blowing gas is cold by cold blowing Gas Cooler when cold blowing
But to entering next procedure after room temperature；
It can will be inhaled at the end of heating when needing larger demand for fuel, continuous supplementation purification gas during circulating-heating
Carbon dioxide in attached tower C in medium, which is diluted to, to meet the requirements, then adsorption tower is not necessarily to pressure release and boost process；The removing day
The process system of carbon dioxide, can not only remove the carbon dioxide in raw natural gas, can also remove raw material day in right gas
Heavy hydrocarbon and moisture in right gas.
Advantageous effect：
1. the present invention is mainly to provide a kind of process system and method for removing carbon dioxide in natural, it is suitable for various natural
Gas source is particularly suitable for the less situation of carbon dioxide in natural gas content, solves when not using distributed energy
Conventional temp.-change adsorptive process carbon dioxide removal can not efficiently use regeneration gas problem.
Present invention is generally directed to the areas of water shortage or land used anxiety, and applicability is good, the LNG device natural gas methane rate of recovery
Height, while the flow of the present invention is simple, investment is small, environmentally friendly, floor space is small, has many advantages, such as easy to operate.
Regeneration gas is passed through circularly-supercharged machine by the present invention in order to solve the problems, such as that regeneration gas is irretrievable in absorption method technique
By regeneration gas circulating-heating so that absorption tower packing heating increases containing for precipitation in adsorption tower during heating with temperature
The natural gas of carbon dioxide enters fuel surge tank, will when heating closes to an end by the adsorption tower pressure release in heated condition
Adsorption tower includes foreign gas and leaks into fuel surge tank, and absorption tower pressure interior force is only slightly higher than fuel surge tank, boosts again later, this
The flow for greatly reducing out system regeneration gas is lifted, the adsorption tower in heated condition after boosting still remains a small amount of titanium dioxide
The impurity such as carbon restart circulating-heating process and heat gas are imported regeneration air cooling to reach further purification purpose
Be incorporated to raw material tracheae after device cooling and enter adsorption process, with ensure these fraction of impure gases will not during cold blowing band
Enter next procedure.
Description of the drawings：
Attached drawing 1 is the flowage structure schematic diagram of the present invention.
Wherein：1, adsorption tower A, 2, adsorption tower B, 3, adsorption tower C, 4, circularly-supercharged machine, 5, heater, 6, accumulation of heat
Device, 7, cold blowing Gas Cooler, 8, regeneration Gas Cooler, 9, fuel gas surge tank.
Specific implementation mode：
Embodiment 1：
A kind of process system of removing carbon dioxide in natural, composition include：Raw natural gas entrance, the raw material day
Right gas entrance is connect with the inlet tube of adsorption tower A1, adsorption tower B2, adsorption tower C3 respectively by valve, adsorption tower A, adsorption tower B,
The outlet of adsorption tower C is connect by valve with purified natural gas pipe, and purified natural gas pipe passes through valve and each cold blowing inlet tube
It is connected, each cold blowing outlet is connected with 7 inlet tube of cold blowing Gas Cooler, cold blowing Gas Cooler outlet and purified natural gas pipe phase
Even, 5 outlet of heater is connected with adsorption tower A, adsorption tower B, adsorption tower C inlet tubes respectively by valve, adsorption tower A, absorption
Tower B, the outlets adsorption tower C stove pipe are connected by valve with 6 inlet tube of storage heater, accumulator outlet pipe and circularly-supercharged machine 4
Inlet tube is connected, and circularly-supercharged machine outlet is connected with heater inlet pipe.
Embodiment 2：
According to a kind of process system of removing carbon dioxide in natural described in embodiment 1, the accumulator outlet pipe is logical
It crosses valve to connect with 9 inlet tube of fuel gas surge tank, the fuel gas surge tank outlet is connect with fuel gas pipe, is heated up
A small amount of mixed gas of adsorption tower removes in journey carbon dioxide and natural gas is as fuel.
Embodiment 3：
A kind of process system of removing carbon dioxide in natural according to embodiment 2, the accumulator outlet pipe with
The connection of 8 inlet tube of Gas Cooler is regenerated, the regeneration gas cooler outlet pipe passes through valve and the raw natural gas pipe
Connection, the circularly-supercharged machine import are arranged purified gas and supplement pipeline.
Embodiment 4：
A kind of process system of removing carbon dioxide in natural according to embodiment 2 or 3, it is the adsorption tower A, described
Adsorption tower B, the adsorption tower C fillers be molecular sieve, molecular sieve and activated carbon multiple-hearth, molecular sieve and silica gel multiple-hearth or
Molecular sieve and other combination of adsorbents, are not limited to other fillers.
Embodiment 5：
The method of the process system of removing carbon dioxide in natural according to one of embodiment 1-4, this method include such as
Lower step：
First the source of raw natural gas be suitable for various natural gases, be particularly suitable for carbon dioxide in natural gas content compared with
Few situation removes carbon dioxide in natural using two towers or three tower temp.-changing adsorptions with circularly-supercharged machine serial flow；
When using three tower temp.-changing adsorptions with circularly-supercharged machine serial flow, accumulator outlet pipe and regeneration gas cooler inlet pipe
It is connected, regeneration gas cooler outlet pipe is connected by valve with raw natural gas pipe, when adsorption tower A is in adsorbed state, absorption
When tower B is in cold blowing state, adsorption tower C is in heated condition, and circularly-supercharged machine starts adsorption tower C and storage heater, heater
Interior natural gas adsorption closed cycle heating is to prevent adsorption tower C pressure superelevation after heating temperature raising, and portion of natural gas passes through
It is discharged into fuel gas surge tank after storage heater, stops circularly-supercharged machine when closing to an end heating cycle and run and close to be in
The air intake valve of heated condition adsorption tower C；In heated condition adsorption tower C pressure releases to the pressure of a little higher than fuel surge tank, inhale
The boosting of adsorption tower C air intake valves is opened after the gas rich in impurity is largely discharged in attached tower C, this process reduces in adsorption tower
Impurity content in gas；
After adsorption tower C boostings, and before system switching in a bit of time,（The a bit of time is basis
Carbon dioxide content and unit scale in raw natural gas determine；）Circularly-supercharged machine is reruned, adsorption tower C continues to locate
In heated condition, circularly-supercharged machine import setting cold blowing gas supplements pipeline, for being replaced with purified gas when heating closes to an end
Gas in adsorption tower, these gases for containing residual carbon dioxide return to raw natural gas import after regeneration Gas Cooler cooling
Pipeline enters adsorption tower A circulation absorptions；The carbon dioxide that residual is excessive in cylinder of next cold blowing stage is avoided to take next work to
Sequence；Adsorption tower C initially enters the cold blowing stage at the end of heating while adsorption tower B is in adsorbed state, and adsorption tower A is in heating
State；It is using Partial cleansing gas that adsorbent in adsorption tower is cooling and cold blowing gas is cooled to room temperature by cold blowing Gas Cooler when cold blowing
Enter next procedure afterwards；When calculating determining cold blowing gas flow more than purification gas flow, may be used circularly-supercharged cold
But mode；
When there is larger demand for fuel, continuous supplementation purification gas during circulating-heating can will inhale at the end of heating
Carbon dioxide in attached tower C in medium, which is diluted to, to meet the requirements, then adsorption tower is not necessarily to pressure release and boost process；The removing day
The process system of carbon dioxide, can not only remove the carbon dioxide in raw natural gas, can also remove raw material day in right gas
Heavy hydrocarbon and moisture in right gas；
This system can not only remove the carbon dioxide in raw natural gas, can also remove raw material it is natural in other impurities such as
Heavy hydrocarbon and moisture, but two sets of systems should be separated into, using same removal methods, heavy hydrocarbon and moisture are first removed, it is rear to remove
Carbon dioxide, even if this is because circular regeneration gas temperature is higher, moisture therein still can be by the micro absorption of molecular sieve to residual
The moisture stayed can influence adsorption effect of the next period to carbon dioxide；
The more traditional wet method decarbonization process of the application, flow is simple, equipment is few, low engineering cost, easy to operate, and traditional is natural
Gas liquefaction device pretreating process, decarbonization process mostly use greatly active MDEA techniques, and MDEA methods are using 45%~50%
MDEA aqueous solutions, and suitable activator is added to improve the absorption rate of carbon dioxide, MDEA is not degradable, has relatively strong
Anti- chemically and thermally degradation capability, corrosivity is small, and steam forces down, and solution cycling rate is low, and hydrocarbon solvability is small, is to answer at present
With widest gas purification handle solvent, especially when in raw natural gas carbon dioxide content it is higher（Typically larger than 1%）
When, which has wide range of applications, and domestic almost all of natural gas liquefaction engineering is all made of MDEA techniques at present, though the technique
So there is outstanding advantages of degree of purification is high, methane losses are small, but complex process, take up a large area, invest it is larger, for day
The relatively low situation of carbon dioxide content in right gas, can also use the method carbon dioxide removal of molecular sieve absorption, but traditional
Molecular sieve absorbing process for the regeneration gas containing carbon dioxide can only be used as generator or gas turbine fuel because carbon containing
Regeneration gas is unlike dehydration regeneration gas, and only by cooling by carbon dioxide separation, absorption method can only adapt to the field using distributed energy
Close, thus limit the use scope of absorption method, for not using the natural gas liquefaction plant of distributed energy, no matter raw material day
Carbon dioxide content height in right gas, the technique that can only use traditional MDEA decarburizations.
In order to solve the problems, such as that regeneration gas is irretrievable in absorption method technique, regeneration gas is by circularly-supercharged machine by regeneration gas
Circulating-heating so that absorption tower packing heating contains carbon dioxide in adsorption tower during heating with what temperature raising was precipitated
Natural gas enter fuel surge tank, heating close to an end when by the adsorption tower pressure release in heated condition, will be in adsorption tower
Impure gas leaks into fuel surge tank, and absorption tower pressure interior force is only slightly higher than fuel surge tank, boosts again later, this measure subtracts significantly
The flow for having lacked system regeneration gas, it is miscellaneous that the adsorption tower in heated condition after boosting still remains a small amount of carbon dioxide etc.
Matter supplements a small amount of purified gas restarting circulating-heating process and imports heat gas again to reach further purification purpose
It is incorporated to raw material tracheae after angry cooler cooling and enters adsorption process, to ensure that these fraction of impure gases will not be in cold blowing
Bring subsequent processing into the process；
The application goes out that system regeneration throughput is small, and a small amount of regeneration gas can be used as molecular sieve heating and warming is used, especially
It is suitble to not use the lower natural gas liquefaction device of the carbon dioxide content of distributed energy；
With 100 × 104Nm3/ d natural gas liquefaction engineerings（It is assumed that carbon dioxide content 0.6% in unstripped gas）For, the present invention with
Traditional handicraft is compared to as follows：
Claims (5)
1. a kind of process system of removing carbon dioxide in natural, composition include：Raw natural gas entrance, it is characterized in that：
The raw natural gas entrance is connect with the inlet tube of adsorption tower A, adsorption tower B, adsorption tower C respectively by valve, adsorption tower
A, adsorption tower B, adsorption tower C outlet connect with purified natural gas pipe by valve, purified natural gas pipe by valve with it is each
Cold blowing inlet tube is connected, and each cold blowing outlet is connected with cold blowing Gas Cooler inlet tube, cold blowing Gas Cooler outlet and purification
Natural gas tube is connected, and heater outlet pipe is connected with adsorption tower A, adsorption tower B, adsorption tower C inlet tubes respectively by valve, absorption
Tower A, adsorption tower B, the outlets adsorption tower C stove pipe are connected by valve with storage heater inlet tube, accumulator outlet pipe and cycle
Supercharger inlet tube is connected, and circularly-supercharged machine outlet is connected with heater inlet pipe.
2. a kind of process system of removing carbon dioxide in natural according to claim 1, it is characterized in that：The storage
Hot device outlet is connect by valve with fuel gas surge tank inlet tube, the fuel gas surge tank outlet and fuel gas pipe
It connects, a small amount of mixed gas of adsorption tower removes in temperature-rise period carbon dioxide and natural gas is as fuel.
3. a kind of process system of removing carbon dioxide in natural according to claim 2, it is characterized in that：The storage
Hot device outlet is connect with regeneration gas cooler inlet pipe, and the regeneration gas cooler outlet pipe passes through valve and the original
Expect that natural gas tube connection, the circularly-supercharged machine import are arranged purified gas and supplement pipeline.
4. a kind of process system of removing carbon dioxide in natural according to claim 2 or 3, it is characterized in that：It is described
Adsorption tower A, the adsorption tower B, the adsorption tower C fillers be molecular sieve, molecular sieve and activated carbon multiple-hearth, molecular sieve
It is combined with activated alumina with silica gel multiple-hearth or molecular sieve.
5. a kind of method of process system using the removing carbon dioxide in natural described in one of claim 1-4, special
Sign is：This method comprises the following steps：
First the source of raw natural gas be suitable for various natural gases, be particularly suitable for carbon dioxide in natural gas content compared with
Few situation removes carbon dioxide in natural using two towers or three tower temp.-changing adsorptions with circularly-supercharged machine serial flow；
When using three tower temp.-changing adsorptions with circularly-supercharged machine serial flow, accumulator outlet pipe and regeneration gas cooler inlet pipe
It is connected, regeneration gas cooler outlet pipe is connected by valve with raw natural gas pipe, when adsorption tower A is in adsorbed state, absorption
When tower B is in cold blowing state, adsorption tower C is in heated condition, and circularly-supercharged machine starts adsorption tower C and storage heater, heater
Interior natural gas adsorption closed cycle heating is to prevent adsorption tower C pressure superelevation after heating temperature raising, and portion of natural gas passes through
It is discharged into fuel gas surge tank after storage heater, stops circularly-supercharged machine when closing to an end heating cycle and run and close to be in
The air intake valve of heated condition adsorption tower C；In heated condition adsorption tower C pressure releases to the pressure of a little higher than fuel surge tank, inhale
The boosting of adsorption tower C air intake valves is opened after the gas rich in impurity is largely discharged in attached tower C, this process reduces in adsorption tower
Impurity content in gas；
After adsorption tower C boostings, and circularly-supercharged machine is reruned in a bit of time before system switching, adsorbed
Tower C keeps heated condition, and circularly-supercharged machine import setting cold blowing gas supplements pipeline, net for being used when heating closes to an end
Change gas in gas displacement sorption tower, these gases for containing residual carbon dioxide return to raw material day after regeneration Gas Cooler cooling
Right gas inlet pipeline enters adsorption tower A circulation absorptions；Avoid the carbon dioxide band that residual is excessive in cylinder of next cold blowing stage
To next process；Adsorption tower C initially enters the cold blowing stage adsorption tower B is in adsorbed state simultaneously at the end of heating, and adsorption tower A
In heated condition；It is using Partial cleansing gas that adsorbent in adsorption tower is cooling and cold blowing gas is cold by cold blowing Gas Cooler when cold blowing
But to entering next procedure after room temperature；
It can will be inhaled at the end of heating when needing larger demand for fuel, continuous supplementation purification gas during circulating-heating
Carbon dioxide in attached tower C in medium, which is diluted to, to meet the requirements, then adsorption tower is not necessarily to pressure release and boost process；The removing day
The process system of carbon dioxide, can not only remove the carbon dioxide in raw natural gas, can also remove raw material day in right gas
Heavy hydrocarbon and moisture in right gas.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109200753A (en) * | 2018-11-13 | 2019-01-15 | 惠州凯美特气体有限公司 | A kind of regeneration technology of improved temperature-change adsorption tower |
| CN109499261A (en) * | 2018-12-03 | 2019-03-22 | 四川天科技股份有限公司 | The removing system and method for CO in a kind of used in proton exchange membrane fuel cell hydrogen |
| CN110243136A (en) * | 2019-04-28 | 2019-09-17 | 昆山市恒安工业气体有限公司 | A kind of combined type natural gas liquefaction device |
| CN114437846A (en) * | 2020-11-04 | 2022-05-06 | 中国石油化工股份有限公司 | Optimization method for natural gas pressure swing adsorption denitrification based on computer |
| CN114768465A (en) * | 2022-03-31 | 2022-07-22 | 上海交通大学 | Multistage overlapping continuous solid adsorption carbon capture system and operation method |
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| CN106085528A (en) * | 2016-06-02 | 2016-11-09 | 成都深冷液化设备股份有限公司 | High-adaptability heavy hydrocarbon removal process |
| CN208829616U (en) * | 2018-06-26 | 2019-05-07 | 兰文旭 | Remove the process system of carbon dioxide in natural |
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| CN106085528A (en) * | 2016-06-02 | 2016-11-09 | 成都深冷液化设备股份有限公司 | High-adaptability heavy hydrocarbon removal process |
| CN208829616U (en) * | 2018-06-26 | 2019-05-07 | 兰文旭 | Remove the process system of carbon dioxide in natural |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109200753A (en) * | 2018-11-13 | 2019-01-15 | 惠州凯美特气体有限公司 | A kind of regeneration technology of improved temperature-change adsorption tower |
| CN109499261A (en) * | 2018-12-03 | 2019-03-22 | 四川天科技股份有限公司 | The removing system and method for CO in a kind of used in proton exchange membrane fuel cell hydrogen |
| CN110243136A (en) * | 2019-04-28 | 2019-09-17 | 昆山市恒安工业气体有限公司 | A kind of combined type natural gas liquefaction device |
| CN114437846A (en) * | 2020-11-04 | 2022-05-06 | 中国石油化工股份有限公司 | Optimization method for natural gas pressure swing adsorption denitrification based on computer |
| CN114437846B (en) * | 2020-11-04 | 2023-01-10 | 中国石油化工股份有限公司 | Optimization method for natural gas pressure swing adsorption denitrification based on computer |
| CN114768465A (en) * | 2022-03-31 | 2022-07-22 | 上海交通大学 | Multistage overlapping continuous solid adsorption carbon capture system and operation method |
| CN114768465B (en) * | 2022-03-31 | 2023-11-28 | 上海交通大学 | Multistage cascade continuous solid adsorption carbon capturing system and operation method |
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