CN113698971A - Method for removing heavy hydrocarbon by using low-temperature rectification method - Google Patents
Method for removing heavy hydrocarbon by using low-temperature rectification method Download PDFInfo
- Publication number
- CN113698971A CN113698971A CN202110917015.4A CN202110917015A CN113698971A CN 113698971 A CN113698971 A CN 113698971A CN 202110917015 A CN202110917015 A CN 202110917015A CN 113698971 A CN113698971 A CN 113698971A
- Authority
- CN
- China
- Prior art keywords
- gas
- heavy hydrocarbon
- natural gas
- flash
- hydrocarbon
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 55
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 55
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 52
- 238000000034 method Methods 0.000 title claims abstract description 40
- 239000007789 gas Substances 0.000 claims abstract description 65
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 64
- 239000003345 natural gas Substances 0.000 claims abstract description 29
- 230000018044 dehydration Effects 0.000 claims abstract description 23
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 23
- 238000001816 cooling Methods 0.000 claims abstract description 13
- 239000007788 liquid Substances 0.000 claims abstract description 13
- 238000001179 sorption measurement Methods 0.000 claims abstract description 9
- 239000001307 helium Substances 0.000 claims description 25
- 229910052734 helium Inorganic materials 0.000 claims description 25
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 claims description 25
- 239000002994 raw material Substances 0.000 claims description 25
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 claims description 20
- 239000012071 phase Substances 0.000 claims description 16
- 238000001704 evaporation Methods 0.000 claims description 15
- 230000008020 evaporation Effects 0.000 claims description 15
- 238000000605 extraction Methods 0.000 claims description 10
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims description 10
- 239000007791 liquid phase Substances 0.000 claims description 10
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 claims description 10
- 229910052753 mercury Inorganic materials 0.000 claims description 10
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 10
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 claims description 10
- 239000004408 titanium dioxide Substances 0.000 claims description 10
- 239000003795 chemical substances by application Substances 0.000 claims description 9
- 239000003949 liquefied natural gas Substances 0.000 claims description 6
- 238000006356 dehydrogenation reaction Methods 0.000 claims description 5
- 238000011084 recovery Methods 0.000 claims description 5
- 230000000694 effects Effects 0.000 abstract description 12
- 230000003313 weakening effect Effects 0.000 abstract description 5
- 230000020335 dealkylation Effects 0.000 description 9
- 238000006900 dealkylation reaction Methods 0.000 description 9
- 238000001035 drying Methods 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 150000001412 amines Chemical class 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 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
- C10L3/106—Removal of contaminants of water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
-
- 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
- B01D53/002—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 condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/64—Heavy metals or compounds thereof, e.g. mercury
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/81—Solid phase processes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B23/00—Noble gases; Compounds thereof
- C01B23/001—Purification or separation processes of noble gases
-
- 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
- C10L3/12—Liquefied petroleum gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/602—Oxides
-
- 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
- B01D2257/60—Heavy metals or heavy metal compounds
- B01D2257/602—Mercury or mercury compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/80—Water
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Biomedical Technology (AREA)
- Health & Medical Sciences (AREA)
- Physics & Mathematics (AREA)
- General Engineering & Computer Science (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- Inorganic Chemistry (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention relates to the technical field of natural gas, in particular to a method for removing heavy hydrocarbon by using a low-temperature rectification method, which comprises the following steps: s1, introducing the natural gas into a high-efficiency separator, and then introducing the natural gas into a dry dehydrator for dehydration; s2, introducing the dehydrated natural gas into a demercuration tower for demercuration treatment; s3, cooling natural gas to-30 ℃ in a heat exchanger, separating liquid through a low-temperature separator, decompressing the gas, entering a heavy hydrocarbon flash tank, and recovering flash gas; and S4, when the step S3 is finished, introducing the gas into a heat exchanger for resetting, and entering a hydrocarbon removing tower for adsorption and heavy hydrocarbon removal after rewarming. The invention has the characteristics of avoiding weakening the demercuration effect, avoiding the condition of large pressure difference of the demercuration tower, ensuring the hydrocarbon removal capability and leading the yield to reach the rated load.
Description
Technical Field
The invention relates to the technical field of natural gas, in particular to a method for removing heavy hydrocarbon by using a low-temperature rectification method.
Background
Natural gas often contains saturated water, natural gas liquids, etc. and to pipeline natural gas from oil and gas fields, in addition to removing solid impurities and free liquids carried therein, it is necessary to remove gas phases and natural gas liquid hydrocarbon components that condense to liquids under the transport conditions. The efficiency of natural gas production can also be influenced by the effects of dehydration and dealkylation, and certain influence is also generated on the service life of equipment, so that efficient dehydration and dealkylation are a guarantee for stable, safe and efficient production of liquefied natural gas. The existing dehydration and heavy hydrocarbon removal process causes large pressure difference to a demercuration tower during working, so that the dehydration and hydrocarbon removal capacity is insufficient, and the yield cannot reach the rated load.
Disclosure of Invention
The invention aims to solve the defects that the yield cannot reach the rated load due to insufficient dehydration and dealkylation capacity caused by large pressure difference of a demercuration tower in the prior art, and provides a method for removing heavy hydrocarbon by using a low-temperature rectification method.
In order to achieve the purpose, the invention adopts the following technical scheme:
a method for removing heavy hydrocarbon by using a low-temperature rectification method is designed, and comprises the following steps:
s1, introducing the natural gas into a high-efficiency separator, and then introducing the natural gas into a dry dehydrator for dehydration;
s2, introducing the dehydrated natural gas into a demercuration tower for demercuration treatment;
s3, cooling natural gas to-30 ℃ in a heat exchanger, separating liquid through a low-temperature separator, decompressing the gas, entering a heavy hydrocarbon flash tank, and recovering flash gas;
and S4, when the step S3 is finished, introducing the gas into a heat exchanger for resetting, and entering a hydrocarbon removing tower for adsorption and heavy hydrocarbon removal after rewarming.
Preferably, the recovery of the flash gas comprises the following steps:
a1, connecting the compressor with a heavy hydrocarbon flash tank, then recovering flash steam by opening the compressor, and dividing the recovered flash steam into three parts for utilization;
a2, cooling the first part of flash evaporation gas to 162-170 ℃ at normal pressure to generate liquefied natural gas;
a3, pressurizing and recovering the second part of flash steam to a long-distance transportation official network, a town official network and a gas station for utilization;
and A4, carrying out helium extraction treatment on the third part of flash evaporation gas.
Preferably, the helium extraction process comprises the following steps:
b1, pressurizing the flash evaporation gas, and then cooling to obtain a liquid phase raw material and a gas phase raw material;
b2, separating the liquid phase raw material from the gas phase raw material, and leading out the gas phase raw material to obtain crude helium;
and B3, carrying out dehydrogenation, dehydration and denitrification treatment on the crude helium to obtain refined helium.
Preferably, the compressor is a reciprocating compressor.
Preferably, the reciprocating compressor has a stepless regulation of 15-150% gas quantity.
Preferably, the mercury removing agent in the mercury removing tower consists of ferric oxide, titanium dioxide and aluminum oxide, wherein the ratio of the ferric oxide to the titanium dioxide to the aluminum oxide is 3:2: 2.
Preferably, the hydrocarbon removing tower is a secondary hydrocarbon removing tower.
The method for removing the heavy hydrocarbon by using the low-temperature rectification method has the beneficial effects that: the dehydration drying is moved to the place between demercuration, so that the condition that the demercuration agent is pulverized due to moisture contained in natural gas is prevented, the weakening of the demercuration effect is avoided, the condition that the pressure difference of a demercuration tower is large is avoided, the hydrocarbon removal capability is ensured, and the yield reaches the rated load.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments.
Example 1
A method for removing heavy hydrocarbon by using a low-temperature rectification method comprises the following steps:
s1, natural gas is introduced into the high-efficiency separator, then the natural gas is introduced into the drying dehydrator for dehydration, and the dehydration drying is moved to the place between demercuration, so that the situation that the demercuration agent is pulverized due to moisture contained in the natural gas is prevented, the weakening of the demercuration effect is avoided, the situation that the pressure difference of a demercuration tower is large is avoided, the demercuration effect is ensured, and meanwhile, the high-efficiency separator is added between the dehydration, so that the problem that the amine liquid of the original system is not completely separated is solved.
S2, introducing the dehydrated natural gas into a demercuration tower for demercuration treatment;
s3, the natural gas enters a heat exchanger to be cooled to-30 ℃, then liquid is separated out through a low-temperature separator, the gas is decompressed and enters a heavy hydrocarbon flash tank, the flash gas is recovered, the adsorption method is changed into a low-temperature rectification method to remove heavy hydrocarbon, the hydrocarbon removal effect is good, and the generation of nitrogen in finished products is reduced.
And S4, when the step S3 is finished, introducing the gas into a heat exchanger for resetting, and entering a hydrocarbon removing tower for adsorption and heavy hydrocarbon removal after rewarming.
The recovery of the flash evaporation gas comprises the following steps:
a1, connecting the compressor with a heavy hydrocarbon flash tank, then recovering flash steam by opening the compressor, and dividing the recovered flash steam into three parts for utilization;
a2, cooling the first part of flash evaporation gas to 162 ℃ at normal pressure to generate liquefied natural gas;
a3, pressurizing and recovering the second part of flash steam to a long-distance transportation official network, a town official network and a gas station for utilization;
and A4, carrying out helium extraction treatment on the flash steam of the third part, and recovering the flash steam, thereby avoiding resource waste.
The helium extraction process comprises the following steps:
b1, pressurizing the flash evaporation gas, and then cooling to obtain a liquid phase raw material and a gas phase raw material;
b2, separating the liquid phase raw material from the gas phase raw material, and leading out the gas phase raw material to obtain crude helium;
and B3, carrying out dehydrogenation, dehydration and denitrification treatment on the crude helium to obtain refined helium.
The compressor is a reciprocating compressor.
The reciprocating compressor has 15% gas quantity stepless regulation, and by adopting the gas quantity stepless regulation, the consumption can be greatly reduced, and the unloading starting can reach the minimum starting torque.
The mercury removing agent in the mercury removing tower consists of ferric oxide, titanium dioxide and aluminum oxide, wherein the ratio of the ferric oxide to the titanium dioxide to the aluminum oxide is 3:2: 2.
The dealkylation tower is a secondary dealkylation tower.
Example 2
A method for removing heavy hydrocarbon by using a low-temperature rectification method comprises the following steps:
s1, natural gas is introduced into the high-efficiency separator, then the natural gas is introduced into the drying dehydrator for dehydration, and the dehydration drying is moved to the place between demercuration, so that the situation that the demercuration agent is pulverized due to moisture contained in the natural gas is prevented, the weakening of the demercuration effect is avoided, the situation that the pressure difference of a demercuration tower is large is avoided, the demercuration effect is ensured, and meanwhile, the high-efficiency separator is added between the dehydration, so that the problem that the amine liquid of the original system is not completely separated is solved.
S2, introducing the dehydrated natural gas into a demercuration tower for demercuration treatment;
s3, the natural gas enters a heat exchanger to be cooled to-30 ℃, then liquid is separated out through a low-temperature separator, the gas is decompressed and enters a heavy hydrocarbon flash tank, the flash gas is recovered, the adsorption method is changed into a low-temperature rectification method to remove heavy hydrocarbon, the hydrocarbon removal effect is good, and the generation of nitrogen in finished products is reduced.
And S4, when the step S3 is finished, introducing the gas into a heat exchanger for resetting, and entering a hydrocarbon removing tower for adsorption and heavy hydrocarbon removal after rewarming.
The recovery of the flash evaporation gas comprises the following steps:
a1, connecting the compressor with a heavy hydrocarbon flash tank, then recovering flash steam by opening the compressor, and dividing the recovered flash steam into three parts for utilization;
a2, cooling the first part of flash evaporation gas to 166 ℃ at normal pressure to generate liquefied natural gas;
a3, pressurizing and recovering the second part of flash steam to a long-distance transportation official network, a town official network and a gas station for utilization;
and A4, carrying out helium extraction treatment on the flash steam of the third part, and recovering the flash steam, thereby avoiding resource waste.
The helium extraction process comprises the following steps:
b1, pressurizing the flash evaporation gas, and then cooling to obtain a liquid phase raw material and a gas phase raw material;
b2, separating the liquid phase raw material from the gas phase raw material, and leading out the gas phase raw material to obtain crude helium;
and B3, carrying out dehydrogenation, dehydration and denitrification treatment on the crude helium to obtain refined helium.
The compressor is a reciprocating compressor.
The reciprocating compressor has 80% gas quantity stepless regulation, and by adopting the gas quantity stepless regulation, the consumption can be greatly reduced, and the unloading starting can be realized to reach the minimum starting torque.
The mercury removing agent in the mercury removing tower consists of ferric oxide, titanium dioxide and aluminum oxide, wherein the ratio of the ferric oxide to the titanium dioxide to the aluminum oxide is 3:2: 2.
The dealkylation tower is a secondary dealkylation tower.
Example 3
A method for removing heavy hydrocarbon by using a low-temperature rectification method comprises the following steps:
s1, natural gas is introduced into the high-efficiency separator, then the natural gas is introduced into the drying dehydrator for dehydration, and the dehydration drying is moved to the place between demercuration, so that the situation that the demercuration agent is pulverized due to moisture contained in the natural gas is prevented, the weakening of the demercuration effect is avoided, the situation that the pressure difference of a demercuration tower is large is avoided, the demercuration effect is ensured, and meanwhile, the high-efficiency separator is added between the dehydration, so that the problem that the amine liquid of the original system is not completely separated is solved.
S2, introducing the dehydrated natural gas into a demercuration tower for demercuration treatment;
s3, the natural gas enters a heat exchanger to be cooled to-30 ℃, then liquid is separated out through a low-temperature separator, the gas is decompressed and enters a heavy hydrocarbon flash tank, the flash gas is recovered, the adsorption method is changed into a low-temperature rectification method to remove heavy hydrocarbon, the hydrocarbon removal effect is good, and the generation of nitrogen in finished products is reduced.
And S4, when the step S3 is finished, introducing the gas into a heat exchanger for resetting, and entering a hydrocarbon removing tower for adsorption and heavy hydrocarbon removal after rewarming.
The recovery of the flash evaporation gas comprises the following steps:
a1, connecting the compressor with a heavy hydrocarbon flash tank, then recovering flash steam by opening the compressor, and dividing the recovered flash steam into three parts for utilization;
a2, cooling the first part of flash evaporation gas to-170 ℃ at normal pressure to generate liquefied natural gas;
a3, pressurizing and recovering the second part of flash steam to a long-distance transportation official network, a town official network and a gas station for utilization;
and A4, carrying out helium extraction treatment on the flash steam of the third part, and recovering the flash steam, thereby avoiding resource waste.
The helium extraction process comprises the following steps:
b1, pressurizing the flash evaporation gas, and then cooling to obtain a liquid phase raw material and a gas phase raw material;
b2, separating the liquid phase raw material from the gas phase raw material, and leading out the gas phase raw material to obtain crude helium;
and B3, carrying out dehydrogenation, dehydration and denitrification treatment on the crude helium to obtain refined helium.
The compressor is a reciprocating compressor.
The reciprocating compressor has 150% gas quantity stepless regulation, and by adopting the gas quantity stepless regulation, the consumption can be greatly reduced, and the unloading starting can be realized to reach the minimum starting torque.
The mercury removing agent in the mercury removing tower consists of ferric oxide, titanium dioxide and aluminum oxide, wherein the ratio of the ferric oxide to the titanium dioxide to the aluminum oxide is 3:2: 2.
The dealkylation tower is a secondary dealkylation tower.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.
Claims (7)
1. A method for removing heavy hydrocarbon by using a low-temperature rectification method is characterized by comprising the following steps:
s1, introducing the natural gas into a high-efficiency separator, and then introducing the natural gas into a dry dehydrator for dehydration;
s2, introducing the dehydrated natural gas into a demercuration tower for demercuration treatment;
s3, cooling natural gas to-30 ℃ in a heat exchanger, separating liquid through a low-temperature separator, decompressing the gas, entering a heavy hydrocarbon flash tank, and recovering flash gas;
and S4, when the step S3 is finished, introducing the gas into a heat exchanger for resetting, and entering a hydrocarbon removing tower for adsorption and heavy hydrocarbon removal after rewarming.
2. The method for removing heavy hydrocarbon by using the cryogenic rectification method as claimed in claim 1, characterized in that the recovery of the flash gas comprises the following steps:
a1, connecting the compressor with a heavy hydrocarbon flash tank, then recovering flash steam by opening the compressor, and dividing the recovered flash steam into three parts for utilization;
a2, cooling the first part of flash evaporation gas to 162-170 ℃ at normal pressure to generate liquefied natural gas;
a3, pressurizing and recovering the second part of flash steam to a long-distance transportation official network, a town official network and a gas station for utilization;
and A4, carrying out helium extraction treatment on the third part of flash evaporation gas.
3. The method for removing heavy hydrocarbon by using the cryogenic rectification method as claimed in claim 2, wherein the helium extraction treatment comprises the following steps:
b1, pressurizing the flash evaporation gas, and then cooling to obtain a liquid phase raw material and a gas phase raw material;
b2, separating the liquid phase raw material from the gas phase raw material, and leading out the gas phase raw material to obtain crude helium;
and B3, carrying out dehydrogenation, dehydration and denitrification treatment on the crude helium to obtain refined helium.
4. The method for removing heavy hydrocarbons by using cryogenic rectification as claimed in claim 2, wherein the compressor is a reciprocating compressor.
5. The method for removing heavy hydrocarbon by using low-temperature rectification method as claimed in claim 3, characterized in that the reciprocating compressor has 15-150% gas quantity stepless regulation.
6. The method for removing heavy hydrocarbons by using a low-temperature rectification method according to claim 1, wherein the mercury removing agent in the mercury removing tower is composed of ferric oxide, titanium dioxide and aluminum oxide, and the ratio of the ferric oxide to the titanium dioxide to the aluminum oxide is 3:2: 2.
7. The method for removing heavy hydrocarbons by using the cryogenic rectification method as recited in claim 1, wherein the hydrocarbon removing tower is a secondary hydrocarbon removing tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110917015.4A CN113698971A (en) | 2021-08-11 | 2021-08-11 | Method for removing heavy hydrocarbon by using low-temperature rectification method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110917015.4A CN113698971A (en) | 2021-08-11 | 2021-08-11 | Method for removing heavy hydrocarbon by using low-temperature rectification method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN113698971A true CN113698971A (en) | 2021-11-26 |
Family
ID=78652400
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110917015.4A Pending CN113698971A (en) | 2021-08-11 | 2021-08-11 | Method for removing heavy hydrocarbon by using low-temperature rectification method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113698971A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117487599A (en) * | 2023-10-24 | 2024-02-02 | 宁夏天利丰能源利用有限公司 | Natural gas dehydration and heavy hydrocarbon removal process |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2010051858A (en) * | 2008-08-26 | 2010-03-11 | Sud-Chemie Catalysts Inc | Absorbent of impurities including mercury, arsenic and sulfur, and method for removing the same |
| CN104061758A (en) * | 2014-07-01 | 2014-09-24 | 天津市振津工程设计咨询有限公司 | Device and method for removing heavy hydrocarbon in natural gas through step-by-step condensation |
| WO2015051363A1 (en) * | 2013-10-04 | 2015-04-09 | University Of Cincinnati | Method and system for removing gaseous mercury in flue gases |
| CN106352657A (en) * | 2016-08-24 | 2017-01-25 | 四川空分设备(集团)有限责任公司 | System and method for extracting helium gas from flashing steam |
| CN109097121A (en) * | 2018-09-14 | 2018-12-28 | 中国石油工程建设有限公司 | A kind of gas dehydration demercuration and mercury recyclable device and method |
-
2021
- 2021-08-11 CN CN202110917015.4A patent/CN113698971A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2010051858A (en) * | 2008-08-26 | 2010-03-11 | Sud-Chemie Catalysts Inc | Absorbent of impurities including mercury, arsenic and sulfur, and method for removing the same |
| WO2015051363A1 (en) * | 2013-10-04 | 2015-04-09 | University Of Cincinnati | Method and system for removing gaseous mercury in flue gases |
| CN104061758A (en) * | 2014-07-01 | 2014-09-24 | 天津市振津工程设计咨询有限公司 | Device and method for removing heavy hydrocarbon in natural gas through step-by-step condensation |
| CN106352657A (en) * | 2016-08-24 | 2017-01-25 | 四川空分设备(集团)有限责任公司 | System and method for extracting helium gas from flashing steam |
| CN109097121A (en) * | 2018-09-14 | 2018-12-28 | 中国石油工程建设有限公司 | A kind of gas dehydration demercuration and mercury recyclable device and method |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117487599A (en) * | 2023-10-24 | 2024-02-02 | 宁夏天利丰能源利用有限公司 | Natural gas dehydration and heavy hydrocarbon removal process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US7192468B2 (en) | Configurations and method for improved gas removal | |
| CN109912379B (en) | Refinery dry gas separation method and device | |
| RU2713556C1 (en) | New production equipment and method of producing liquefied hydrogen and liquefied natural gas | |
| CA2482159C (en) | Configurations and methods for improved acid gas removal | |
| CN104419464B (en) | Dry gas recovery system and dry gas recovery method for refinery plant | |
| CN108641769B (en) | Recovery method of oilfield associated gas | |
| CN109749780B (en) | Device and method for recovering carbon dioxide in refinery dry gas by oil absorption and compression condensation method | |
| US11125499B2 (en) | Process for optimizing removal of condensable components from a fluid | |
| CN104087357B (en) | A kind of method and system that heavy hydrocarbon is removed from gas deliquescence process | |
| CN101575254A (en) | Process for recycling polymer grade ethylene from refinery dry gas | |
| CN104061758A (en) | Device and method for removing heavy hydrocarbon in natural gas through step-by-step condensation | |
| CN113698971A (en) | Method for removing heavy hydrocarbon by using low-temperature rectification method | |
| CN104194852A (en) | High-yield light hydrocarbon recovery method from low-pressure natural gas | |
| CN205473626U (en) | System for retrieve heavy hydrocarbon in liquefied natural gas production | |
| CN105733721B (en) | A kind of method and system removing heavy hydrocarbon from natural gas | |
| CN104495751A (en) | Method and device for preparing hydrogen and carbon monoxide by efficient synthesis gas separation | |
| JP2015533636A (en) | A method for optimizing condensable component removal from fluids | |
| CN104560194B (en) | Refinery saturated dry gas recovery system and recovery method | |
| CN116839310A (en) | Process method for preparing food-grade liquid carbon dioxide by utilizing decarburization exhaust gas of LNG (liquefied Natural gas) plant | |
| CN209098595U (en) | A kind of associated gas condensate recovery device for offshore marginal oilfield | |
| CN104826445B (en) | Separating process for recycling start-up tail gas of ethylene compression refrigerating system | |
| CN212299543U (en) | Waste heat utilization device of phenol ammonia recovery system | |
| CN117146527A (en) | Helium extracting device and method for low-temperature rectification of flash gas of liquefied natural gas | |
| CN205473627U (en) | System for desorption heavy hydrocarbon in follow natural gas | |
| CN105779052B (en) | The method and system of heavy hydrocarbon is recycled in a kind of liquefied natural gas (LNG) production |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20211126 |
|
| RJ01 | Rejection of invention patent application after publication |