CN109381985A - A kind of purifying treatment method of natural gas - Google Patents

A kind of purifying treatment method of natural gas Download PDF

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Publication number
CN109381985A
CN109381985A CN201811391655.0A CN201811391655A CN109381985A CN 109381985 A CN109381985 A CN 109381985A CN 201811391655 A CN201811391655 A CN 201811391655A CN 109381985 A CN109381985 A CN 109381985A
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gas
absorption tower
regenerator
absorbing liquid
natural gas
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王建宏
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Beijing Institute of Petrochemical Technology
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Beijing Institute of Petrochemical Technology
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    • 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
    • B01D53/86—Catalytic processes
    • B01D53/8603—Removing sulfur compounds
    • B01D53/8612—Hydrogen sulfide
    • 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
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • 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
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/02—Preparation of sulfur; Purification
    • C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
    • 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
    • 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
    • B01D2257/30—Sulfur compounds
    • B01D2257/304—Hydrogen sulfide
    • 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
    • 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
    • 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
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
    • 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
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Organic Chemistry (AREA)
  • Sustainable Development (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

The invention discloses a kind of purifying treatment methods of natural gas, first higher boiling, low viscosity non-aqueous organic solvent in dissolve Complexing Iron, preparation obtains the organic solution of Complexing Iron；The organic solution is fitted into absorption tower, gas to be processed is made to be bubbled the discharge at the top of the absorption tower after demister demisting of the gas into the absorption tower, after the absorption tower purified treatment from bottom to top by distribution device in gas-fluid from absorb the bottom of the tower；The absorbing liquid for absorbing sour gas is pumped into regenerator regeneration in the bottom on the absorption tower, and the absorbing liquid after regeneration is re-fed into the absorption tower by pump and is recycled；Sulphur in regenerator is from bottommost timing outlet, Recovered sulphur after filtering, and filtrate returns again to the regenerator and recycles.The method achieve desulfurization, decarburization and dehydrations simultaneously, and the target that absorbing liquid recycles, and no discharging of waste liquid, regeneration energy consumption is low, and simple process, occupied area is small, and operating cost is low.

Description

A kind of purifying treatment method of natural gas
Technical field
The present invention relates to natural gas purification technical field more particularly to a kind of purifying treatment methods of natural gas.
Background technique
It is net that the natural gas that the natural gas or coal gas come out from mine generates need to successively pass through desulfurization and decarburization, dehydration etc. Change is handled, and after the quality standard for reaching commercial natural gas, can just be conveyed to user, alcohol is widely used in selexol process decarburization at present The united method of amine-Crouse, process are the H in natural gas2S、CO2It is absorbed in aqueous alkanolamine Deng first, then, decompression Or heating richness H2S/CO2Aqueous alkanolamine, reach regeneration hydramine, flash distillation CO2, concentration H2The purpose of S, the severe toxicity after concentration H2S passes through Claus device Recovered sulphur, the SO of Claus device discharge2Tail gas also needs further to purify, to reach environmental protection Standard, the natural gas after desulfurization and decarburization can just be pipelined to final use after recycling triethylene glycol or molecular sieve dehydration Family.
Natural gas purification technology in the prior art, not only take up a large area, purification process it is extremely complex, but also be cleaned into This is also higher, if purification/liquefaction cost of liquefied natural gas accounts for the 30%-40% of natural gas supply cost, with environmental protection It is stringent, the purification cost of natural gas will further improve.
Summary of the invention
The object of the present invention is to provide a kind of purifying treatment methods of natural gas, and the method achieve desulfurization, decarburization simultaneously And dehydration, and the target that absorbing liquid recycles, no discharging of waste liquid, regeneration energy consumption is low, and simple process, occupied area is small, operation It is at low cost.
The purpose of the present invention is what is be achieved through the following technical solutions:
A kind of purifying treatment method of natural gas, which comprises
Step 1, first higher boiling, low viscosity non-aqueous organic solvent in dissolve Complexing Iron, preparation obtains Complexing Iron Organic solution；
The organic solution is fitted into absorption tower by step 2, is distributed gas to be processed by gas from absorb the bottom of the tower Device is bubbled from bottom to top into the absorption tower, the gas after the absorption tower purified treatment after demister demisting from Discharge at the top of the absorption tower；
Step 3, the absorbing liquid for absorbing sour gas are pumped into regenerator regeneration in the bottom on the absorption tower, then Absorbing liquid after life is re-fed into the absorption tower by pump and is recycled；
Sulphur in step 4, the regenerator is from bottommost timing outlet, Recovered sulphur after filtering, and filtrate returns again to The regenerator recycles.
In step 1, the Complexing Iron is containing [Fe (edta)]-The iron complex of anion；
The higher boiling, low viscosity non-aqueous organic solvent include boiling point 180 DEG C or more it is highly polar, complexing can be dissolved The liquid organic compound or ionic liquid of iron.
In step 2, process of the gas to be processed in the absorption tower purified treatment specifically:
H in the gas to be processed2S is oxidized to sulphur and H by the Complexing Iron in the organic solution+, while Complexing Iron It is ferrous to be reduced to complexing；
CO in the gas to be processed2And H2O is synchronous by the organic solution Physical Absorption.
In step 3, the absorbing liquid for absorbing sour gas is in the regenerated process of regenerator specifically:
Oxygen-fed gas is bubbled by distribution device in gas-fluid enters the regenerator, and the ferrous complex in absorbing liquid is described Dioxygen oxidation in oxygen-fed gas is iron complex, while the CO in absorbing liquid2And H2O is by the oxygen-fed gas stripping, then passes through Outlet after demister.
The volume of the oxygen-fed gas needs 5 times more excessive or more than theoretical amount.
Operation temperature in the absorption tower and regenerator is no more than 100 DEG C.
As seen from the above technical solution provided by the invention, the above method realizes while desulfurization, decarburization and dehydration, And the target that absorbing liquid recycles, no discharging of waste liquid, regeneration energy consumption is low, and simple process, occupied area is small, and operating cost is low, It is all important breakthrough to energy-saving and emission-reduction, by-product resource etc..
Detailed description of the invention
In order to illustrate the technical solution of the embodiments of the present invention more clearly, required use in being described below to embodiment Attached drawing be briefly described, it should be apparent that, drawings in the following description are only some embodiments of the invention, for this For the those of ordinary skill in field, without creative efforts, it can also be obtained according to these attached drawings other Attached drawing.
Fig. 1 provides the purifying treatment method flow diagram of natural gas for the embodiment of the present invention；
Fig. 2 is the process schematic of example desulfurization of the present invention, decarburization and dehydration.
Specific embodiment
With reference to the attached drawing in the embodiment of the present invention, technical solution in the embodiment of the present invention carries out clear, complete Ground description, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.Based on this The embodiment of invention, every other implementation obtained by those of ordinary skill in the art without making creative efforts Example, belongs to protection scope of the present invention.
The embodiment of the present invention is described in further detail below in conjunction with attached drawing, is implemented as shown in Figure 1 for the present invention Example provides the purifying treatment method flow diagram of natural gas, which comprises
Step 1, first higher boiling, low viscosity non-aqueous organic solvent in dissolve Complexing Iron, preparation obtains Complexing Iron Organic solution；
In the step, the Complexing Iron is containing [Fe (edta)]-The iron complex of anion；
The higher boiling, low viscosity non-aqueous organic solvent include that boiling point flows under 180 DEG C or more highly polar, room temperature Liquid organic compound or ionic liquid functional, that Complexing Iron can be dissolved.
Here, absorbent at least two parts part forms, i.e., high boiling organic matter and capable of being dissolved in high boiling has The Complexing Iron of machine object.High boiling organic matter main function is physical dissolved hydrogen sulfide, carbon dioxide, water and oxygen, simultaneously It is required that as small as possible to the solubility of the hydro carbons such as methane；The effect of Complexing Iron is catalysis oxidation hydrogen sulfide.
The organic solution is fitted into absorption tower by step 2, is distributed gas to be processed by gas from absorb the bottom of the tower Device is bubbled from bottom to top into the absorption tower, the gas after the absorption tower purified treatment after demister demisting from Discharge at the top of the absorption tower；
In the step, process of the gas to be processed in the absorption tower purified treatment specifically:
H in the gas to be processed2S is oxidized to sulphur and H by the Complexing Iron in the organic solution+, while Complexing Iron It is ferrous to be reduced to complexing；
CO in the gas to be processed2And H2O is synchronous by the organic solution Physical Absorption.
Specifically, the desulfurization principle in absorption tower are as follows:
H2S is absorbed by liquid absorption: H2S(g)→H2S(l)
H2Complexing Iron oxidation in S absorbed liquid: 2Fe3+L+H2S(l)→2Fe2+L+S+2H+
The overall reaction of Complexing Iron catalysis oxidation hydrogen sulfide are as follows:
2H2S(l)+O2(l)→2S+2H2O
Decarburization principle in absorption tower are as follows:
CO2It is absorbed by liquid absorption: CO2(g)→CO2(l)
Dewatering Principle in absorption tower are as follows:
H2O is absorbed by liquid absorption: H2O(g)→H2O(l)。
Step 3, the absorbing liquid for absorbing sour gas are pumped into regenerator regeneration in the bottom on the absorption tower, then Absorbing liquid after life is re-fed into the absorption tower by pump and is recycled；
In the step, the absorbing liquid for absorbing sour gas is in the regenerated process of regenerator specifically:
Oxygen-fed gas is bubbled by distribution device in gas-fluid enters the regenerator, and the ferrous complex in absorbing liquid is described Dioxygen oxidation in oxygen-fed gas is iron complex, while the CO in absorbing liquid2And H2O is by the oxygen-fed gas stripping, then passes through Outlet after demister.
Specifically, the Complexing Iron regeneration principle in regenerator are as follows:
O2It is absorbed by liquid absorption: O2(g)→O2(l)
O2Complexing ferrous oxidation Fe in absorbed liquid2+L+O2(l)+4H+→4Fe3+L+2H2O
Carbon dioxide stripping principle in regenerator are as follows:
CO in absorbing liquid2By excessive oxygen-fed gas stripping: CO2(l)→CO2(g)
Water stripping principle in regenerator are as follows:
H in absorbing liquid2O is by excessive oxygen-fed gas stripping: H2O(l)→H2O(g)
Recycling for organic solvent and Complexing Iron is realized by principles above.
In the specific implementation, the volume of the oxygen-fed gas is needed than excessively 5 times or more of theoretical amount.
Operation temperature in above-mentioned absorption tower and regenerator is no more than 100 DEG C.
Sulphur in step 4, the regenerator is from bottommost timing outlet, Recovered sulphur after filtering, and filtrate returns again to The regenerator recycles.
In the specific implementation, the effect of the distribution device in gas-fluid in absorption tower and regenerator is to generate micro-bubble, improves and inhale Receipts and reproduction speed, but either absorption column of gas or regenerator, have the generation of sulphur, distribution device in gas-fluid is necessary It is avoided that the blocking of sulphur.
The effect of demister in absorption tower and regenerator is the spilling for avoiding organic solvent with air-flow, is reduced organic molten The loss of agent.
During desulfurization, Complexing Iron plays the role of liquid phase oxidation catalysis, and reaction is substantially the H in natural gas2S Oxygen in equal sulfur-containing compounds and oxygen-fed gas generates sulphur and water, theoretically natural gas integrated desulfurization, decarburization and de- What hydraulic art uniquely consumed is oxygen-fed gas.
Above-described embodiment the method is described in detail with specific example below, is illustrated in figure 2 institute of the present invention Give an actual example the process schematic of desulfurization, decarburization and dehydration, with reference to Fig. 2:
Sour natural gas to be processed enters bubble absorbing tower, CO therein by gas distributor from bottom2, the quilts such as water Higher boiling non-aqueous media Physical Absorption, H2The sulfur-containing compounds such as S generate sulphur by the Complexing Iron oxidative absorption in non-aqueous media, together When Complexing Iron to be reduced to complexing ferrous；
Purified sour gas is discharged at the top of absorption tower after demisting；
Absorb H2S、CO2It is sent to regenerator regeneration with the absorbing liquid of water, the complexing ferrous iron in non-aqueous media is passed through gas The oxygen-fed gas that body distributor blasts is regenerated as Complexing Iron, the CO in absorbing liquid2It is also realized and regenerates by oxygen-fed gas stripping with water, Non-aqueous media containing Complexing Iron is transported to absorption tower again and is recycled.
Specifically to purify for example:
The dimethyl sulphoxide solution (weight of iron concentration is 2.5607g/L) of a certain amount of NaFe (edta) is placed in absorption tower, It is passed through the CO of 20mL, 156Kpa, 99.99% (v/v)2, balance is reached in 2.5 minutes, uptake is that every g absorbing liquid absorbs 0.0101g CO2, then start to regenerate, is passed through 95mL into regenerator, behind air 2.5 minutes of 156Kpa, CO2Regeneration rate 100%.
The dimethyl sulphoxide solution (weight of iron concentration is 2.5607g/L) of a certain amount of NaFe (edta) is placed in absorption tower, It is passed through the CO of the 20mL, 156Kpa, 99% (v/v) that are saturated with water2, balance is reached in 1560 minutes, every g absorbing liquid absorbs CO2With H2The quality of O is 0.5816g, then starts to regenerate, and is passed through 95mL into regenerator, behind air 1020 minutes of 156Kpa, CO2 And H2The regeneration rate 100% of O.
The dimethyl sulphoxide solution (weight of iron concentration is 2.5607g/L) of a certain amount of NaFe (edta) is placed in absorption tower, Flow is the H of 99.9% (v/v) of 10mL/min2S is passed through absorption tower, and flow is 99.9% (v/v) O of 25mL/min2It is passed through again Raw tower, while catalysis oxidation is carried out, after 4 hours, 1L absorbent generates 55.4g sulphur.
It is worth noting that, the above method can individually remove hydrogen sulfide or carbon dioxide, or remove simultaneously hydrogen sulfide and Carbon dioxide, or hydrogen sulfide, carbon dioxide and water are removed simultaneously.
It is worth noting that, the content being not described in detail in the embodiment of the present invention belongs to professional and technical personnel in the field's public affairs The prior art known.
In conclusion the method for the embodiment of the present invention has the advantages that
1) realize at the same desulfurization, decarburization and dehydration it is integrated, greatly reduce occupied area and equipment investment.
2) the Complexing Iron organic solvent system of the present embodiment realizes quickly again during desulfurization, decarburization and dehydration It is raw, it recycles, reduces the operating cost of whole process.
3) product of this process is high-purity sulphur, realizes the resource utilization of waste.
The foregoing is only a preferred embodiment of the present invention, but scope of protection of the present invention is not limited thereto, Within the technical scope of the present disclosure, any changes or substitutions that can be easily thought of by anyone skilled in the art, It should be covered by the protection scope of the present invention.Therefore, protection scope of the present invention should be with the protection model of claims Subject to enclosing.

Claims (6)

1. a kind of purifying treatment method of natural gas, which is characterized in that the described method includes:
Step 1, first higher boiling, low viscosity non-aqueous organic solvent in dissolve Complexing Iron, preparation obtains the organic of Complexing Iron Solution；
The organic solution is fitted into absorption tower by step 2, and gas to be processed is made to pass through distribution device in gas-fluid from absorb the bottom of the tower It is bubbled from bottom to top and enters the absorption tower, the gas after the absorption tower purified treatment is after demister demisting from described Discharge at the top of absorption tower；
Step 3, the absorbing liquid for absorbing sour gas are pumped into regenerator regeneration in the bottom on the absorption tower, after regeneration Absorbing liquid be re-fed into the absorption tower by pump and recycled；
Sulphur in step 4, the regenerator is from bottommost timing outlet, Recovered sulphur after filtering, and filtrate return again to it is described Regenerator recycles.
2. the purifying treatment method of natural gas according to claim 1, which is characterized in that in step 1,
The Complexing Iron is containing [Fe (edta)]-The iron complex of anion；
The higher boiling, low viscosity non-aqueous organic solvent include boiling point 180 DEG C or more it is highly polar, Complexing Iron can be dissolved Liquid organic compound or ionic liquid.
3. the purifying treatment method of natural gas according to claim 1, which is characterized in that in step 2, the gas to be processed Process of the body in the absorption tower purified treatment specifically:
H in the gas to be processed2S is oxidized to sulphur and H by the Complexing Iron in the organic solution+, while Complexing Iron is gone back It originally was that complexing is ferrous；
CO in the gas to be processed2And H2O is synchronous by the organic solution Physical Absorption.
4. the purifying treatment method of natural gas according to claim 1, which is characterized in that in step 3, described to absorb acid The absorbing liquid of property gas is in the regenerated process of regenerator specifically:
Oxygen-fed gas is bubbled by distribution device in gas-fluid enters the regenerator, and the ferrous complex in absorbing liquid is by the oxygen supply Dioxygen oxidation in gas is iron complex, while the CO in absorbing liquid2And H2O is by the oxygen-fed gas stripping, then passes through demisting Outlet after device.
5. the purifying treatment method of natural gas according to claim 4, which is characterized in that
The volume of the oxygen-fed gas needs 5 times more excessive or more than theoretical amount.
6. the purifying treatment method of natural gas according to claim 1, which is characterized in that
Operation temperature in the absorption tower and regenerator is no more than 100 DEG C.
CN201811391655.0A 2018-11-21 2018-11-21 A kind of purifying treatment method of natural gas Pending CN109381985A (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112604457A (en) * 2020-12-09 2021-04-06 北京化工大学 Process for dehydrating natural gas by using mixed solvent of ionic liquid and triethylene glycol
CN113088360A (en) * 2021-04-20 2021-07-09 中国海洋石油集团有限公司 Natural gas desulfurization absorption tower device of offshore floating production platform

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US20140140912A1 (en) * 2011-06-21 2014-05-22 Friedrich-Alexander-Universitaet Erlangen-Nuernber Catalytic oxidation of sulphide species
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CN107569990A (en) * 2016-07-05 2018-01-12 北京化工大学苏州（相城）研究院 The depriving hydrogen sulphide of sulfurous gas-efficient oxidation regeneration integrated method and system
CN107812450A (en) * 2017-12-07 2018-03-20 北京石油化工学院 A kind of method of alkaline nonaqueous phase wet method catalysis oxidation hydrogen sulfide

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102019141A (en) * 2010-12-20 2011-04-20 昆明理工大学 Process for purifying tail gas containing hydrothion by using liquid phase catalytic oxidation method
US20140140912A1 (en) * 2011-06-21 2014-05-22 Friedrich-Alexander-Universitaet Erlangen-Nuernber Catalytic oxidation of sulphide species
CN103691274A (en) * 2013-11-14 2014-04-02 中国石油化工股份有限公司 Method for production regulation of chelated iron desulfurization process
CN105080316A (en) * 2014-04-29 2015-11-25 北京化工大学 Desulfurizer used for removing H2S and method for removing H2S
CN107569990A (en) * 2016-07-05 2018-01-12 北京化工大学苏州（相城）研究院 The depriving hydrogen sulphide of sulfurous gas-efficient oxidation regeneration integrated method and system
CN107812450A (en) * 2017-12-07 2018-03-20 北京石油化工学院 A kind of method of alkaline nonaqueous phase wet method catalysis oxidation hydrogen sulfide

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112604457A (en) * 2020-12-09 2021-04-06 北京化工大学 Process for dehydrating natural gas by using mixed solvent of ionic liquid and triethylene glycol
CN113088360A (en) * 2021-04-20 2021-07-09 中国海洋石油集团有限公司 Natural gas desulfurization absorption tower device of offshore floating production platform

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Application publication date: 20190226