CN109370670B - Process system for simultaneously removing carbon dioxide, water and heavy hydrocarbon in natural gas - Google Patents

Process system for simultaneously removing carbon dioxide, water and heavy hydrocarbon in natural gas Download PDF

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CN109370670B
CN109370670B CN201811092634.9A CN201811092634A CN109370670B CN 109370670 B CN109370670 B CN 109370670B CN 201811092634 A CN201811092634 A CN 201811092634A CN 109370670 B CN109370670 B CN 109370670B
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adsorption tower
gas
cold blowing
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carbon dioxide
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兰文旭
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/106—Removal of contaminants of water
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/102—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
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/104—Alumina
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • 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

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Separation Of Gases By Adsorption (AREA)
  • Drying Of Gases (AREA)

Abstract

Simultaneously remove carbon dioxide, moisture and heavy hydrocarbon's among the natural gas process system. The traditional dry pretreatment process is simple, is not suitable for pretreatment with high carbon dioxide content, and the wet process is complex, and the alcohol amine reagent is toxic, and the solution and desalted water need to be supplemented regularly. The invention comprises the following components: adsorption tower I (1), adsorption tower II (2), adsorption tower III (3), it links to each other with cold blow import pipe to purify natural gas pipe through valve I (10), cold blow outlet pipe links to each other with cold blow gas cooler (9) import pipe, cold blow gas cooler outlet pipe links to each other with cold blow gas booster compressor (8) import pipe, cold blow gas booster compressor outlet pipe is connected with cold blow import pipe and purification trachea respectively, adsorption tower I, adsorption tower II, adsorption tower III middle part has the export, export heating gas pipe passes through the valve and imports union coupling with heat accumulator (4), the heat accumulator outlet pipe is imported union coupling with heating gas booster compressor (5). The invention is used for the process system for simultaneously removing carbon dioxide, water and heavy hydrocarbon in natural gas.

Description

Process system for simultaneously removing carbon dioxide, water and heavy hydrocarbon in natural gas
The technical field is as follows:
the invention relates to the technical field of natural gas pretreatment in a natural gas liquefaction technology, in particular to a process system and a method for simultaneously removing carbon dioxide, water and heavy hydrocarbon in natural gas. .
Background art:
natural gas is a high-quality energy source which is green, environment-friendly, economical, safe and reliable, the research on a natural gas purification process in the natural gas liquefaction technology is also important for the development of the natural gas industry, and components with higher freezing points in the natural gas, such as carbon dioxide, moisture, heavy hydrocarbon and the like, can be solidified and block equipment in the natural gas liquefaction process, and must be removed before liquefaction; the traditional pretreatment method is to remove acid gases such as carbon dioxide and hydrogen sulfide by an alcohol amine method, adsorb and remove water and heavy hydrocarbon by a molecular sieve and activated carbon composite bed, for an LNG plant with larger fuel demand such as a gas turbine driving compressor or gas power generation or a downstream pipe network, when the content of carbon dioxide in raw material gas is lower and is usually lower than 1%, a dry pretreatment process can be adopted, namely the molecular sieve and the activated carbon composite bed adsorb and simultaneously remove water, heavy hydrocarbon and carbon dioxide, and a small amount of regenerated gas (accounting for 7-15% of the treatment gas volume) is used for power generation or the downstream pipe network; when the content of carbon dioxide is high, the amount of the regenerated gas is larger than the demand of power generation, and the redundant carbon-containing regenerated gas cannot be recycled because the carbon dioxide cannot be separated by a cooling method, and only can enter a torch to be discharged, so that waste is caused; therefore, the traditional dry pretreatment process is simple in flow, convenient to operate and low in investment, but is not suitable for pretreatment of natural gas with high carbon dioxide content; only the traditional wet process can be adopted; the wet natural gas pretreatment process has the disadvantages of complex flow, various equipment, large investment and toxic alcohol amine reagent, and the solution and desalted water need to be supplemented periodically during operation.
The invention content is as follows:
the invention aims to provide a process method for simultaneously removing carbon dioxide, moisture and heavy hydrocarbon in natural gas, which has simple flow and strong applicability, and adopts a series flow of three-tower Temperature Swing Adsorption (TSA) and a heated gas booster to simultaneously remove carbon dioxide gas or other impurities in the natural gas.
The above purpose is realized by the following technical scheme:
a process system for simultaneously removing carbon dioxide, water and heavy hydrocarbon in natural gas comprises the following components: adsorption tower I, adsorption tower II, adsorption tower III, characterized by: the adsorption tower I, the adsorption tower II and the inlet pipe of the adsorption tower III are connected with a feed gas inlet through a valve, the adsorption tower I, the adsorption tower II and the outlet pipe of the adsorption tower III are connected with a purification gas pipe through a valve, the purification natural gas pipe is connected with a cold blowing inlet pipe through a valve I, the cold blowing outlet pipe is connected with a cold blowing gas cooler inlet pipe, the cold blowing gas cooler outlet pipe is connected with a cold blowing supercharger inlet pipe, the cold blowing supercharger outlet pipe is respectively connected with the cold blowing inlet pipe and the purification gas pipe, outlets are arranged in the middle of the adsorption tower I, the adsorption tower II and the adsorption tower III, an outlet heating gas pipe is connected with a heat accumulator inlet pipe through a valve, and a heat accumulator outlet pipe is connected with a heating gas supercharger inlet pipe, and the outlet pipe of the heating gas booster is connected with the inlet pipe of the heater.
The process system for simultaneously removing carbon dioxide, moisture and heavy hydrocarbon in natural gas is characterized in that an inlet pipe of an adsorption tower I, an inlet pipe of an adsorption tower II and an outlet pipe of the bottom of the adsorption tower III are connected with an inlet pipe of a heating gas cooler through valves, and an outlet pipe of the heating gas cooler is connected with a fuel gas pipe.
The process system for simultaneously removing carbon dioxide, moisture and heavy hydrocarbon in natural gas is characterized in that the inlet pipe of the heat accumulator is connected with the inlet pipe of the cold blowing gas cooler through a valve II, and the outlet pipe of the cold blowing gas cooler is connected with the cold blowing gas booster.
Desorption natural gas in the time carbon dioxide, moisture and heavy hydrocarbon's process systems, adsorption tower I adsorption tower II adsorption tower III divide into two-stage bed, the lower extreme bed is used for desorption moisture and heavy hydrocarbon, fill molecular sieve and active carbon composite filler, molecular sieve and silica gel composite filler or molecular sieve and active alumina composite filler combination, the upper end bed is used for desorption carbon dioxide, fills 13X molecular sieve, also can be divided into two adsorption towers of establishing ties with every adsorption tower according to the circumstances, moisture and heavy hydrocarbon are got rid of to first tower, second tower desorption carbon dioxide.
The process system for simultaneously removing carbon dioxide, water and heavy hydrocarbon in natural gas comprises the following steps:
firstly, the source of raw material gas is suitable for various natural gases, and water, heavy hydrocarbon and carbon dioxide impurities in the natural gases are removed by adopting a series flow of three-tower temperature swing adsorption and a circulating supercharger;
the method comprises the following steps of adopting a series flow of three-tower temperature swing adsorption and a circulating booster, when an adsorption tower I is in an adsorption state and an adsorption tower II is in a cold blowing state, enabling an adsorption tower III to be in a heating state, starting the cold blowing gas circulating booster to circularly cool the adsorption tower II, and supplementing purified gas through a valve I to maintain pressure along with temperature reduction and pressure reduction caused by supplementing fuel gas to a heating gas pipeline in a circulating cooling process; when the calculated cold blowing amount is less than or equal to the flow of the purified gas, the cold blowing circulation supercharger can be eliminated, and all the purified gas is used as cold blowing and then returns to the purified gas pipeline from the outlet of the cold blowing cooler, so that the flow is simplified; the heating gas supercharger is started to circularly heat the natural gas in the upper section of the adsorption tower III, the heat accumulator and the heater, and the other part of the heating gas flows through the lower section of the adsorption tower from the upper section of the adsorption tower, is heated, dehydrated and subjected to heavy hydrocarbon removal bed layers, enters the heating gas cooler to be cooled, and then is sent out as fuel or enters a downstream pipeline network; this heated gas is supplemented by valve II in the line. Due to the continuous supplement of the gases, the carbon dioxide in the heating gas in the cyclic heating process at the upper section of the adsorption tower can be gradually diluted and meets the purification requirement; and switching after the adsorption period is reached, heating the adsorption tower I, adsorbing by the adsorption tower II, cold blowing by the adsorption tower III, and circulating.
Has the advantages that:
1. the invention mainly provides a process system and a method for simultaneously removing carbon dioxide, water and heavy hydrocarbon in natural gas, which are suitable for small and medium-sized natural gas liquefaction plants which are self-generating or have downstream natural gas pipe networks, solves the defects of complex process flow, large device investment, large occupied area, need of desalted water and the like in the traditional wet decarburization and dry dehydration heavy hydrocarbon removal process, and simultaneously solves the problems that the regenerated gas is larger than the fuel gas and cannot be completely consumed by adopting a common dry pretreatment process.
The heat accumulator is arranged in front of the heating gas booster, so that the heating energy consumption is reduced by about 25%, and the heating gas cooler and the cooling energy consumption are saved.
According to the invention, different heating modes are set according to the characteristic that the difference between the heating air quantity needed by the decarburization part and the heating air quantity needed by the dehydration part is larger, the decarburization part with larger heating air quantity carries out cyclic heating regeneration, the dehydration and heavy hydrocarbon removal part with smaller heating air quantity adopts the traditional heating mode, the adsorption and cold blowing processes are the same, two sets of systems are organically combined, a large number of switching valves and partial equipment are saved, the cost is reduced, and the reason that the dehydration part and the decarburization part can not be cyclically heated together needs to be pointed out, because moisture exists in the cyclically heated regeneration gas, the moisture can still be slightly adsorbed in a 13X molecular sieve in the decarburization bed layer although the heating temperature is higher, and the adsorption effect of carbon dioxide in the next period is.
Description of the drawings:
FIG. 1 is a schematic diagram of the flow structure of the present invention.
Wherein: 1. the system comprises adsorption towers I and 2, adsorption towers II and 3, adsorption towers III and 4, a heat accumulator 5, a heating gas booster 6, a heater 7, a heating gas cooler 8, a cold blowing gas booster 9, a cold blowing gas cooler 10, cold blowing gas supplementing valves I and 11 and a heating gas supplementing valve II.
The specific implementation mode is as follows:
example 1:
a process system for simultaneously removing carbon dioxide, water and heavy hydrocarbon in natural gas comprises the following components: adsorption column I1, adsorption column II2, adsorption column III3, characterized by: the adsorption tower I, the adsorption tower II, the inlet pipe of the adsorption tower III is connected with a feed gas inlet through a valve, the adsorption tower I, the adsorption tower II, the outlet pipe of the adsorption tower III is connected with a purification gas pipe through a valve, the purification natural gas pipe is connected with a cold blowing inlet pipe through a valve I10, the cold blowing outlet pipe is connected with a cold blowing gas cooler 9 inlet pipe, the cold blowing gas cooler outlet pipe is connected with a cold blowing supercharger 8 inlet pipe, the cold blowing supercharger outlet pipe is respectively connected with the cold blowing inlet pipe and the purification gas pipe, the adsorption tower I, the adsorption tower II and the adsorption tower III are provided with an outlet (the bottom of a carbon dioxide removal bed) in the middle part, the outlet heating gas pipe is connected with a heat accumulator 4 inlet pipe through a valve, and the heat accumulator outlet pipe is connected with a heating gas supercharger 5 inlet pipe, the outlet pipe of the heating gas booster is connected with the inlet pipe of the heater 6.
Example 2:
according to the process system for removing carbon dioxide, moisture and heavy hydrocarbon in natural gas simultaneously in embodiment 1, outlet pipes at the bottoms of the adsorption tower I, the adsorption tower II and the adsorption tower III are connected with an inlet pipe of a heating gas cooler 7 through valves, an outlet pipe of the heating gas cooler is connected with a fuel gas pipe, and a small amount of mixed gas of carbon dioxide and natural gas removed by the adsorption tower in the temperature rising process is used as fuel.
Example 3:
according to the process system for simultaneously removing carbon dioxide, moisture and heavy hydrocarbon in natural gas in the embodiment 2, the inlet pipe of the heat accumulator is connected with the inlet pipe of the cold blowing gas cooler through the valve II11 to serve as supplementary heating gas, and the outlet pipe of the cold blowing gas cooler is connected with the cold blowing gas booster.
Example 4:
according to embodiment 2 or 3 desorption carbon dioxide in natural gas, moisture and heavy hydrocarbon's processing system simultaneously, adsorption tower I adsorption tower II adsorption tower III divide into two-stage bed, lower extreme bed is used for desorption moisture and heavy hydrocarbon, fill molecular sieve and active carbon composite filler, molecular sieve and silica gel composite filler or molecular sieve and active alumina composite filler combination, upper end bed is used for desorption carbon dioxide, fill 13X molecular sieve, also can divide into two adsorption towers of establishing ties with every adsorption tower according to the circumstances, moisture and heavy hydrocarbon are got rid of to first tower, carbon dioxide is got rid of to second tower.
Example 5:
the process system for simultaneously removing carbon dioxide, water and heavy hydrocarbons in natural gas according to embodiments 1-4, the method of the process system comprising the steps of:
firstly, the source of raw material gas is suitable for various natural gases, and water, heavy hydrocarbon and carbon dioxide impurities in the natural gases are removed by adopting a series flow of three-tower temperature swing adsorption and a circulating supercharger;
the method comprises the following steps of adopting a series flow of three-tower temperature swing adsorption and a circulating booster, when an adsorption tower I is in an adsorption state and an adsorption tower II is in a cold blowing state, enabling an adsorption tower III to be in a heating state, starting the cold blowing gas circulating booster to circularly cool the adsorption tower II, and supplementing purified gas through a valve I to maintain pressure along with temperature reduction and pressure reduction caused by supplementing fuel gas to a heating gas pipeline in a circulating cooling process; when the calculated cold blowing amount is less than or equal to the flow of the purified gas, the cold blowing circulation supercharger can be eliminated, and all the purified gas is used as cold blowing and then returns to the purified gas pipeline from the outlet of the cold blowing cooler, so that the flow is simplified; the heating gas supercharger is started to circularly heat the natural gas in the upper section of the adsorption tower III, the heat accumulator and the heater, and the other part of the heating gas flows through the lower section of the adsorption tower from the upper section of the adsorption tower, is heated, dehydrated and subjected to heavy hydrocarbon removal bed layers, enters the heating gas cooler to be cooled, and then is sent out as fuel or enters a downstream pipeline network; this heated gas is supplemented by valve II in the line. Due to the continuous supplement of the gases, the carbon dioxide in the heating gas in the cyclic heating process at the upper section of the adsorption tower can be gradually diluted and meets the purification requirement; switching after the adsorption period is reached, heating the adsorption tower I, adsorbing by the adsorption tower II, cold blowing by the adsorption tower III, and circulating;
compared with the traditional wet decarburization process, the process is simple, the equipment is few, the construction cost is low, the operation is convenient, the traditional pretreatment process of the natural gas liquefaction device is mostly an active MDEA process, the MDEA method adopts a 45-50% MDEA aqueous solution, and a proper amount of activating agent is added to improve the absorption rate of carbon dioxide, the MDEA is not easy to degrade, has strong chemical and thermal degradation resistance, small corrosivity, low vapor pressure, low solution circulation rate and small hydrocarbon dissolving capacity, is a gas purification treatment solvent which is most widely applied at present, almost all natural gas liquefaction projects at home and abroad adopt the MDEA process at present, although the process has the outstanding advantages of high purification degree, small methane loss and the like, the process is complex, the occupied area is large, the investment is large, and the process aims at natural gas liquefaction plants with self-power generation or downstream natural gas pipe networks, a dry pretreatment process can also be adopted, but the conventional dry process has limited application range of natural gas with high carbon dioxide content (generally more than 1%) because the quantity of the regenerated gas exceeds the fuel demand of a generator or a gas turbine, and the regenerated gas cannot be completely consumed.
At 30 × 104Nm3For example,/d natural gas liquefaction engineering (assuming 2% carbon dioxide content in the feed gas), the invention is compared with the traditional process as follows:
Figure DEST_PATH_IMAGE001
it can be seen from the table that, of the indexes, only one of the energy consumption is not as good as the traditional mode, but only the heat consumption of the primary energy is slightly higher, and the power consumption of the secondary energy is better than the traditional mode. For the project of adopting the self-generating electricity or the gas turbine to drive the compressor, the generator has a large amount of tail gas waste heat, and the heat is not counted in the cost, so the invention has obvious advantages.

Claims (2)

1. A system for simultaneously removing carbon dioxide, water and heavy hydrocarbons in natural gas comprises: adsorption tower I, adsorption tower II, adsorption tower III, characterized by: inlet pipes of the adsorption tower I, the adsorption tower II and the adsorption tower III are connected with a raw material gas inlet through valves, outlet pipes of the adsorption tower I, the adsorption tower II and the adsorption tower III are connected with a purified gas pipe through valves, the purification air pipe is connected with the cold blowing inlet pipe through a valve I, the cold blowing outlet pipe is connected with the cold blowing air cooler inlet pipe, the outlet pipe of the cold blowing gas cooler is connected with the inlet pipe of the cold blowing gas booster, the outlet pipe of the cold blowing gas booster is respectively connected with the cold blowing inlet pipe and the purifying gas pipe, the middle parts of the adsorption tower I, the adsorption tower II and the adsorption tower III are provided with outlets, outlet heating gas pipes are connected with inlet pipes of the heat accumulator through valves, the outlet pipe of the heat accumulator is connected with the inlet pipe of the heating gas booster, and the outlet pipe of the heating gas booster is connected with the inlet pipe of the heater;
outlet pipes at the bottoms of the adsorption tower I, the adsorption tower II and the adsorption tower III are connected with an inlet pipe of a heated gas cooler through valves, and an outlet pipe of the heated gas cooler is connected with a fuel gas pipe;
the inlet pipe of the heat accumulator is connected with the inlet pipe of the cold blowing gas cooler through a valve II, and the outlet pipe of the cold blowing gas cooler is connected with a cold blowing gas booster;
adsorption tower I adsorption tower II adsorption tower III divide into two-stage bed, the lower extreme bed is used for desorption moisture and heavy hydrocarbon, fill molecular sieve and active carbon composite filler, molecular sieve and silica gel composite filler or molecular sieve and active alumina composite filler combination, the upper end bed is used for desorption carbon dioxide, fills 13X molecular sieve, divide every adsorption tower into the adsorption tower of two series connections, first tower desorption moisture and heavy hydrocarbon, second tower desorption carbon dioxide.
2. A method for removing carbon dioxide, water and heavy hydrocarbons from natural gas by using the system for simultaneously removing carbon dioxide, water and heavy hydrocarbons as claimed in claim 1, wherein the system comprises: the method comprises the following steps:
firstly, the source of raw gas is suitable for various natural gases, and water, heavy hydrocarbon and carbon dioxide impurities in the natural gas are removed by adopting a series flow of three-tower temperature swing adsorption and a circulating supercharger;
the method comprises the following steps of adopting a series flow of three-tower temperature swing adsorption and a circulating booster, when an adsorption tower I is in an adsorption state and an adsorption tower II is in a cold blowing state, enabling an adsorption tower III to be in a heating state, starting the cold blowing gas circulating booster to circularly cool the adsorption tower II, and supplementing purified gas through a valve I to maintain pressure along with temperature reduction and pressure reduction caused by supplementing fuel gas to a heating gas pipeline in a circulating cooling process; when the calculated cold blowing amount is less than or equal to the flow of the purified gas, a cold blowing circulation supercharger is cancelled, and all the purified gas is used as cold blowing and then returns to a purified gas pipeline from the outlet of a cold blowing cooler, so that the flow is simplified;
the heating gas supercharger is started to circularly heat the natural gas in the upper section of the adsorption tower III, the heat accumulator and the heater, and the other part of the heating gas flows through the lower section of the adsorption tower from the upper section of the adsorption tower, is heated, dehydrated and subjected to heavy hydrocarbon removal bed layers, enters the heating gas cooler to be cooled, and then is sent out as fuel or enters a downstream pipeline network; the heating gas is supplemented by a valve II in the pipeline, and due to the continuous supplement of the gas, the carbon dioxide in the heating gas at the upper section of the adsorption tower in the cyclic heating process can be gradually diluted and meets the purification requirement; and switching after the adsorption period is reached, heating the adsorption tower I, adsorbing by the adsorption tower II, cold blowing by the adsorption tower III, and circulating.
CN201811092634.9A 2018-09-20 2018-09-20 Process system for simultaneously removing carbon dioxide, water and heavy hydrocarbon in natural gas Expired - Fee Related CN109370670B (en)

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