CN215712846U - Natural gas dry-type purifier - Google Patents
Natural gas dry-type purifier Download PDFInfo
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- CN215712846U CN215712846U CN202121020342.1U CN202121020342U CN215712846U CN 215712846 U CN215712846 U CN 215712846U CN 202121020342 U CN202121020342 U CN 202121020342U CN 215712846 U CN215712846 U CN 215712846U
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Abstract
The utility model relates to a natural gas dry-type purification device, which comprises a gravity separator, a filtering separator and a dry-type purification reaction container which are sequentially arranged; the dry type purification reactor is characterized in that a modified adsorbent bed layer is arranged in the dry type purification reactor, the upper side of the dry type purification reactor is connected with a dust filter, the top of the dry type purification reactor is connected with a heat exchange device, the bottom of the dry type purification reactor is connected with a conversion device, a catalyst container is arranged in the conversion device, and a plurality of dry type purification reactors are connected in parallel. The raw material natural gas is conveyed to a gravity separator through a pressurizing station, the gravity separator is used for filtering and separating the raw material natural gas, after impurity removal, water removal and hydrocarbon liquid removal, the raw material natural gas enters a dry purification reaction vessel, sulfide in the raw material natural gas is adsorbed and purified through a modified adsorbent bed layer filled in the dry purification reaction vessel, and the purified natural gas meets the requirements of the national latest standard 'natural gas' GB17820-2018 on the sulfide content of a type of natural gas.
Description
Technical Field
The utility model relates to the technical field of natural gas treatment, in particular to a dry type natural gas purifying device.
Background
Natural gas, as a relatively clean energy source, contains small amounts of sulfur compounds, such as inorganic sulfur H2S, and organic sulfur: COS, CS2Mercaptans, thioethers, etc., the presence of which makes sulfur dioxide in flue gas not reach the standard when natural gas is used as fuel for combustion. Meanwhile, the existence of sulfide can generate corrosive substances, and the natural gas pipeline is corroded and damaged by long-term transportation and storage. At present, the national standard GB17820-2018 of China already stipulates the sulfur content in a natural gas as follows: h2S content is less than or equal to 6mg/m3Total sulfides (in terms of sulfur) is less than or equal to 20mg/m3. The same or higher standards are also found for the corresponding sulfur contents in natural gas in the European standard EN 16726-2016 and the German standard DVGW G260-2013.
At present, the method for desulfurizing and purifying natural gas mainly adopts a dry adsorption method taking solid as an adsorbent and a solvent absorption method taking liquid as an adsorbent, and the two adsorption modes are characterized in that: and (3) removing sulfides in the natural gas by combining physical adsorption and chemical reaction. The two natural gas desulfurization and purification modes have respective advantages and disadvantages, for example, when dry adsorption (method) is adopted and molecular sieve is mainly used as an adsorbent, the molecular sieve has stronger adsorption H2S capacity, but the adsorption effect on organic sulfur is general, and COS and CS in natural gas2And when the content of organic sulfur such as mercaptan is high, the sulfur content of the purified natural gas cannot be realizedThe amount reaches the standard, secondly, the molecular sieve has stronger water absorption, and has stronger dehydration effect while desulfurizing, and water molecules occupy the surface of the molecular sieve to absorb H2Micropores of S, influence molecular sieves on H2Adsorption capacity of S, water and H2The coexistence of S also affects the regeneration performance of the molecular sieve. When solvent absorption is used, a portion of the chemical solvent is available for CO2And H2S is not selective, resulting in excessive solvent filling and reduced economic benefit, and a part of chemical solvent is also used for H2S has strong selective adsorption, but for COS and CS2The adsorption capacity of organic sulfur such as mercaptan is poor, the desulfurization purification mode has the defects in process, and besides the purification mode, the adsorbent is mainly monopolized by various overseas companies such as UOP, Dow, Pasteur and the like, so that the economic benefit is poor.
SUMMERY OF THE UTILITY MODEL
The utility model solves the technical problem that sulfides in natural gas are removed in a dry type renewable purification mode, the problems in the prior art are solved by combining the prior purification device and working conditions according to the characteristics of a natural gas purification section device, and the natural gas dry type purification device is arranged to effectively and simultaneously remove organic sulfur, such as COS and CS, in the natural gas2Mercaptans, thioethers, etc., and inorganic sulfur H2S, the sulfide content in the natural gas reaches the requirement of national standard GB17820-2018 of natural gas on the sulfide content in the natural gas, namely H2S content is less than or equal to 6mg/m3Total sulfides (in terms of sulfur) is less than or equal to 20mg/m3。
The technical route of the utility model is as follows: the raw material natural gas from a booster station is subjected to impurity removal by a gravity separator, is dehydrated by a filtering separator and is subjected to hydrocarbon liquid removal, then enters a dry-type purification reaction vessel, passes through a modified adsorbent bed layer in the (dry-type purification) reaction vessel, is subjected to purification adsorption by a (modified) adsorbent bed layer, and has the sulfur content (by weight of sulfur element) of less than 20mg/m in the natural gas passing through the (modified) adsorbent bed layer3,H2S content is less than or equal to 6mg/m3Meets the national standard requirement, and the clean natural gas passes through the dust filterAfter treatment, the product natural gas can be used as product natural gas for users, when the (modified) adsorbent bed layer is saturated, the reaction container in which the saturated adsorbent is positioned is switched to an analytic state, and the purified sulfur content is less than 20mg/m3Heating clean natural gas or nitrogen, introducing the thermal desorption gas source into a saturated modified adsorbent bed layer in a reaction container to perform thermal desorption regeneration of the adsorbent, cold blowing the regenerated adsorbent, standing for recycling, repeating the above process, converting the organic sulfur into H by using saturated regeneration gas containing sulfide after being converted by a catalyst in a conversion device2And S, introducing the oil and gas plant desulfurization device for desulfurization treatment.
A natural gas dry-type purification device comprises a gravity separator, a filtering separator and a dry-type purification reaction container which are sequentially arranged; the dry type purification reaction vessel is internally provided with a modified adsorbent bed, the upper side of the dry type purification reaction vessel is connected with a dust filter, the top of the dry type purification reaction vessel is connected with a heat exchange device, the bottom of the dry type purification reaction vessel is connected with a conversion device, the conversion device is internally provided with a catalyst vessel, the dry type purification reaction vessels are connected in parallel, one part of the dry type purification reaction vessels can be in an adsorption state, and the other part of the dry type purification reaction vessels can be in an analysis state in the same time period.
Furthermore, 2-12 dry purification reaction vessels are arranged in parallel.
Still further, all be provided with the valve on each part connecting tube of device.
Still further, the dry purification reaction vessel comprises 2 first dry purification reaction vessels and 2 second dry purification reaction vessels which are arranged in parallel, wherein a first modified adsorbent bed layer is arranged in the first dry purification reaction vessel, and a second modified adsorbent bed layer is arranged in the second dry purification reaction vessel.
Still further, a plurality of first modified adsorbent beds are arranged in the first dry-type purification reaction vessel, and a plurality of second modified adsorbent beds are arranged in the second dry-type purification reaction vessel; when the dry type purification reaction vessel is in an adsorption state, natural gas raw gas enters the dry type purification reaction vessel and passes through the modified adsorbent bed from bottom to top; when the dry type purification reaction vessel is in a desorption state, the heated desorption gas source passes through the saturated modified adsorbent bed layer from top to bottom.
Still further, the dry purification reaction vessel can be selected from various types of reaction vessels, the reaction vessel comprises an axial or radial fixed bed, and further, a vertical or horizontal reaction vessel can be selected, so that the system pressure drop requirement and the site field limitation are met.
Still further, the dry-type purification reactor contains a gas distribution device, optionally the gas distribution device is a guide plate, and further, a modified adsorbent bed layer is supported and fixed by using ceramic ball packing, wherein the ceramic balls play a certain gas distribution role, so that the raw material (natural) gas and the thermal desorption (natural) gas uniformly pass through the modified adsorbent bed layer.
Still further, the modified adsorbent of the modified adsorbent bed layer is one or a combination of two of a modified molecular sieve and modified activated carbon.
Preferably, the modified adsorbent takes one or more of a 3A type molecular sieve, a 4A type molecular sieve, a 5A type molecular sieve, a 13X type molecular sieve, a RK-29 molecular sieve, a RK-33 molecular sieve, coconut shell activated carbon, coal-based activated carbon and wood activated carbon as a substrate, and is modified by one or more of alkali metal, alkali metal oxide, transition metal oxide, rare earth metal and noble metal.
Still further, when the dry (purification) reaction vessel is in an adsorption state, the raw natural gas is directly passed through the (modified) adsorbent bed without being pressurized or heated, and when the dry (purification) reaction vessel is in a desorption state, the desorbed (natural) gas is heated to 200 to 450 ℃ and is passed through the saturated (modified) adsorbent bed to thermally desorb and regenerate the saturated adsorbent. The analysis process can be dry-type purification with sulfur content less than 20mg/m3The purified natural gas or nitrogen is heated by a heat exchange device to reach 200-450 ℃, and preferably, the heat exchange device is a tube type heat exchanger, a plate type heat exchanger, an electric heater or a heater according to the arrangement and heat source of a field deviceOne or several synergistic effects of the heat furnace, and further, the desorption regeneration gas is input into the dry (purification) reaction vessel with saturated (modified adsorbent) bed layer after depressurization. Introducing the saturated regenerated gas after the analysis process into a conversion device, and carrying out hydrogenolysis conversion by a catalyst to saturate COS and CS in the regenerated gas2With H in natural gas2Is converted into H by hydrogenolysis catalyst2And S, further, conveying the regenerated gas subjected to hydrogenolysis conversion to a desulfurization device of an oil and gas plant for treatment.
The catalyst for assisting the hydrogenolysis conversion of the saturated regeneration gas is one or more of substrate materials such as a silicon-aluminum-soil base, an active alumina base, an active carbon base and the like, and one or more of active substances such as alkali metals, alkaline earth metals, rare earth metals, noble metals and the like are carried by the modes of dipping, mixing, coating and the like, and further, the catalyst is one or a combination of a columnar shape and a honeycomb body.
The purification process of the device comprises the following steps:
removing impurities from raw natural gas from a booster station through a gravity separator, dehydrating through a filtering separator, and feeding into a dry purification reaction vessel;
step two, the raw material natural gas after the preliminary dust removal and dehydration treatment enters a dry purification reaction vessel, passes through a modified adsorbent bed layer in the dry purification reaction vessel, and is purified and adsorbed by a fixed modified adsorbent bed layer to remove inorganic sulfur H2S, organic sulfur COS, CS2Mercaptans, thioethers, conversion of H in natural gas2The content of S is reduced to be less than or equal to 6mg/m3Reducing the total sulphide content to less than or equal to 20mg/m, calculated as sulphur3Outputting the natural gas desulfurized and purified by the dry-type purification reaction vessel to a dust filter, and using the purified natural gas output from the dust filter as product gas for users to use;
step three, when the adsorbent of the modified adsorbent bed layer in the dry purification reaction vessel is saturated, switching the dry purification reaction vessel from an adsorption state to an desorption state, heating the purified natural gas or nitrogen gas purified in the step one and the step two through a heat exchange device, introducing the heated desorption regeneration gas source into the adsorbent of the saturated modified adsorbent bed layer, performing thermal desorption regeneration of the adsorbent, introducing normal-temperature clean natural gas or nitrogen gas into the modified adsorbent bed layer after desorption regeneration, purging and cooling, standing the dry purification reaction vessel after cold blowing for 0.5-2 hours, and switching to the adsorption state;
step four, introducing saturated regeneration gas into the conversion device, wherein most of organic sulfur in the saturated regeneration gas comprises COS and CS2By catalytic conversion to H2S, the saturated regeneration gas output by the conversion device contains a large amount of H2S and a very small amount of COS, and the converted saturated regeneration gas is sent to a desulfurization device of an oil and gas plant for treatment.
Further, the dry purification process of the natural gas is characterized by comprising the following steps:
in the first step, 700m at 300 ℃ is used3The total sulfide content in terms of sulfur is less than 20mg/m3Heating the adsorbent of the saturated first modified adsorbent bed and the first dry purification reaction vessel by using clean natural gas for 2.5 hours;
second, 100m at 300 ℃ is used3The first modified adsorbent bed temperature was maintained for a total of 2.5 hours with clean natural gas;
thirdly, closing the heat exchange device, and introducing 700m with the normal temperature of 35 ℃ into the first dry-type purification reaction container3The first modified adsorbent bed is cooled and blown by clean natural gas, and the process lasts for 2.5 hours;
and fourthly, stopping introducing the clean natural gas into the first dry type purification reaction vessel, allowing the first modified adsorbent bed layer to stand for 0.5 hour, returning the first dry type purification reaction vessel to the initial state after the regeneration process is carried out for 8 hours, and completing the regeneration of the modified adsorbent of the first modified adsorbent bed layer so as to be put into an adsorption state for use.
Further, when the first dry purification reaction vessel is in an adsorption state for 8 hours and the first modified adsorbent bed in the reaction vessel of the first dry purification reaction vessel is saturated by adsorption, the first dry purification reaction vessel is switched to the desorption stateThe state of the second dry-type purification reaction vessel is switched to an adsorption state, and the raw material natural gas is 10000m3The gas source enters a gravity separator to remove impurities, enters a filtering separator to be dehydrated, and the acid impurities form a dry gas source without large particle impurities, enters a second dry purification reaction vessel, sulfides contained in the natural gas source are removed through a second modified adsorbent bed layer, and the desulfurized natural gas enters a dust filter to remove dust carried out of the second modified adsorbent bed layer and serves as a clean natural gas source for users;
when the first dry-type cleaning reaction vessel is switched to the analysis state, 700m3The total sulfide content in terms of sulfur is less than 20mg/m3A clean natural gas source enters a heat exchange device), the clean natural gas source is heated to 250-350 ℃, the adsorbent entering a first modified adsorbent bed layer of a saturated first dry-type purification reaction container is blown and penetrated through the first modified adsorbent bed layer to ensure that the adsorbent bed layer is thermally resolved and regenerated, a saturated resolved gas source is discharged from the bottom of the first dry-type purification reaction container and enters a conversion device, and organic sulfur including COS and CS in the saturated resolved gas source is dissolved and desorbed through a bed layer of a hydrogenolysis conversion catalyst container2Through hydrogenolysis conversion, the hydrogen reacts with natural gas desorption gas source hydrogen to generate H2And S, forming a converted saturated regenerated gas source by the natural gas desorbed gas subjected to hydrogenolysis conversion, and conveying the converted saturated regenerated gas source to a desulfurization device of an oil and gas plant for treatment.
The utility model has the technical effects that: the utility model relates to a method for removing H in natural gas2S，COS，CS2The utility model relates to a device for mercaptan and thioether, which ensures that the pure natural gas meets the requirement of the latest national standard 'natural gas' GB17820-2018 on the sulfide content of a natural gas, namely H2S content is less than or equal to 6mg/m3Total sulfides (in terms of sulfur) is less than or equal to 20mg/m3The natural gas purified by the dry-type natural gas purifying device can be used as product gas for transportation and use by end users.
Drawings
FIG. 1 is a schematic view of the apparatus of the present invention;
the equipment indicated by the reference numbers in the above figures is as follows:
1. the system comprises a first gas source pipeline, a second gas source pipeline, a first valve, a gravity separator, a second valve, a filtering separator, a second gas source pipeline, a second valve, a third valve, a first modified adsorbent bed, a first dry purification reaction vessel, a second valve, a third valve, a fourth valve, a fifth valve, a third valve, a fifth valve, a sixth valve, a seventh valve, a second dry purification reaction vessel, a third valve, a fourth valve, a fifth valve, a sixth valve, a seventh valve, a 15, a second dry purification reaction vessel, a eighth valve, a fourth valve, a sixth valve, a fourth valve, a ninth valve, a sixth valve, a 25, a sixth valve, a dust filter, a sixth valve, a fourteenth valve, a fifteenth valve.
Detailed Description
The embodiment is explained as an explanation of the utility model, is not the only implementation way of the utility model, and is not a limitation on the implementation way and the implementation range of the utility model, and the non-innovative process improvement based on the utility model and the process optimization without changing the main equipment and the adsorbent are both in the protection scope of the utility model.
The utility model relates to a natural gas dry-type purification device, wherein raw natural gas is conveyed to a gravity separator 3 through a pressurizing station, a filter separator 5 is used for removing impurities, water and hydrocarbon liquid, the raw natural gas enters a dry-type purification reaction vessel, sulfide in the raw natural gas is adsorbed and purified through a modified adsorbent bed layer filled in a (dry-type purification) reaction vessel, the natural gas purified through the (modified adsorbent) bed layer is used for removing dust carried out by the raw natural gas through the (modified) adsorbent bed layer through a dust filter 26, and the purified natural gas meets the requirements of the latest national standard GB17820-2018 on the sulfide content of natural gas, namely H2S content is less than or equal to 6mg/m3Total sulfides (in terms of sulfur) is less than or equal to 20mg/m3The natural gas purified by the dry-type natural gas purifying device can be used as product gas for transportation and use by end users.
The modified adsorbent saturated by adsorption can be thermally analyzed and regenerated by heating, maintaining temperature, cold blowing, standing, etc., and using clean air source, such as total sulfur content less than 20mgm3The saturated regeneration gas is converted by the catalyst in the conversion device 22, and the organic sulfur in the saturated regeneration gas is converted into H2And S, introducing the saturated regeneration desorption gas subjected to hydrogenolysis catalytic conversion into a desulfurization device of an oil and gas plant for desulfurization treatment. The modified adsorbent is prepared by taking one or more of 3A type molecular sieve, 4A type molecular sieve, 5A type molecular sieve, 13X type molecular sieve, RK-29 molecular sieve, RK-33 molecular sieve, coconut shell activated carbon, coal-based activated carbon and wood activated carbon as a substrate and modifying one or more of alkali metal, alkali metal oxide, transition metal oxide, rare earth metal and noble metal through the modes of dipping, mixing, coating and the like.
Specifically, the dry-type natural gas purification device comprises a gravity separator 3, a filtering separator 5, a modified adsorbent, a dry-type purification reaction container, a conversion device 25, a catalyst, a heat exchange device 25 and a dust filter 26. The dry purification reaction vessels are 2 to 12 and are arranged in parallel, raw material natural gas can be simultaneously shunted to pass through all or part of the dry purification reaction vessels, so that one part of the dry purification reaction vessels is in an adsorption state, the other part of the dry purification reaction vessels is in an analytic state, the dry purification reaction vessels have two states, namely the adsorption state and the analytic state, and the dry purification reaction vessels can be selected from vertical or horizontal reaction vessels to adapt to system pressure drop and site limitation. When the (dry purification) reaction vessel is in an adsorption state, the raw material natural gas is not subjected to temperature rise and pressurization treatment, when the (dry purification) reaction vessel is in an desorption state, the purified natural gas or the nitrogen desorption gas with the temperature of 200-450 ℃ is heated to 200-450 ℃ and penetrates through the saturated (modified) adsorbent, so that the adsorbent is thermally desorbed and regenerated, after the adsorbent is regenerated, the desorption gas with the temperature of 15-40 ℃ at normal temperature penetrates through the heated adsorbent, the (modified) adsorbent bed is cooled and blown, then the gas source is cut off, and after the normal temperature adsorbent bed is kept still, the dry purification reaction vessel can be switched to the adsorption state again to purify the raw material natural gas.
Further, in the analysis process, an air source is heated to 200-450 ℃ through a heat exchange device 25, the heat exchange device 25 is arranged according to public and auxiliary media of a site and a plant area, and one or more of a tubular heat exchanger, a plate heat exchanger, an electric heater and a heating furnace are selected to act synergistically.
Further, the desorbed regeneration gas is depressurized and fed to a dry (clean) reactor vessel saturated with a (modified adsorbent) bed. Organic sulfur in the regenerated gas (or regenerated gas) is subjected to hydrogenolysis conversion by a catalyst (arranged in a catalyst container 23) in a conversion device 22 to generate H2And S, conveying the gas after catalytic conversion to a desulfurization device of an oil and gas plant for treatment. The catalyst is one or more of columnar or honeycomb catalyst, and the substrate of the catalyst is one or more of (substrate) materials such as silica-alumina, activated carbon and the like, and carries one or more of active substances such as alkali metal, alkaline earth metal, rare earth metal, noble metal and the like.
The dry purification process of the natural gas based on the device comprises the following steps:
step one, outputting raw material natural gas through a pressurizing station, removing impurities and dehydrating through a gravity separator 3 and a filtering separator 4, and conveying to a dry-type purification reaction container.
Step two, the raw material natural gas penetrates through the modified adsorbent bed layer in the dry purification reaction vessel to remove the sulfide, such as H, in the raw material gas2S、COS、CS2Mercaptan, thioether, etc. are removed and treated by dust filter 26 to make the sulfur content in natural gas as product gas reach H2S content is less than or equal to 6mg/m3The total sulfide content (in terms of sulfur) is less than or equal to 20mg/m3。
Step three, when the (modified) adsorbent is saturated in the process of the step three, the (dry purification) reaction container is switched from the adsorption state to the desorption state, the clean natural gas or the nitrogen purified in the step one and the step two is heated by the heat exchange device 25, the thermal desorption gas penetrates through the saturated (modified) adsorbent bed layer to carry out thermal desorption adsorption, the desorbed (modified) adsorbent is blown and cooled by the normal-temperature clean natural gas or the nitrogen, and the (dry purification) reaction container subjected to the supercooling blowing process is switched to the adsorption state after standing.
Step four, introducing the regeneration gas source into the conversion device 22 after the regeneration gas source penetrates through (modifies) the adsorbent bed, and generating H through catalytic conversion of most organic sulfur in the saturated regeneration gas2S, containing a large amount of H output from the conversion device 222And S and a small amount of organic sulfur regeneration gas are conveyed to a desulfurization device of an oil and gas plant for purification treatment.
Specifically, the dry type natural gas purification device provided by the utility model solves the problem of H removal of raw natural gas2S，COS，CS2And sulfide such as mercaptan, thioether and the like are removed by arranging a gravity separator 3, a filtering separator 5 and a plurality of dry-type purification reaction containers after a raw material natural gas conveying device through the adsorption effect of a modified adsorbent (bed layer), the purified natural gas is used as product natural gas after being treated by a dust filter 26, the saturated adsorbent can be analyzed by clean natural gas heated by a heat exchange device 25, the saturated analysis gas is subjected to catalyst hydrogenolysis catalysis, and organic sulfur is converted into H2S, introducing the natural gas into a desulfurization device of an oil and gas plant for treatment, and alternately switching the adsorption state and the desorption state of a plurality of dry purification reaction containers, wherein the natural gas treated by the dry purification process can meet the requirement of national standard GB17820-2018 on the content of sulfide in a natural gas, namely H2S content is less than or equal to 6mg/m3Total sulfides (in terms of sulfur) is less than or equal to 20mg/m3。
Hereinafter, an embodiment of the present invention will be described by using 2 dry purification reactors (first dry purification reactor 10 and second dry purification reactor 15) as an example of the basic embodiment of the present invention alternately, and in fact, 2 to 12 identical dry (purification) reactors may be provided in parallel depending on the total amount of raw material natural gas, so that natural gas may equally pass through some or all of the reactors, and some of the dry purification reactors may be in an adsorption state and some of the dry purification reactors may be in an analysis state.
The embodiment provides a natural gas dry-type purifier:
the pressure from the booster station was 4500 fKPa, raw natural gas 10000m at 35 deg.C3And/h, the natural gas enters the gravity separator 3 through the first gas source pipeline 1 and the first valve 2 to remove impurities, enters the filtering separator 5 through the second valve (valve) 4 to be dehydrated and a certain amount of acidic impurities to form a dry gas source without large-particle impurities, enters the first dry purification reaction vessel 10 through the second valve 7 and the third valve 8 through the second gas source pipeline 6, sulfide contained in the natural gas source passing through the second gas source pipeline 6 is removed through the first modified adsorbent bed layer 9, the desulfurized natural gas enters the dust filter 26 through the sixth valve 13 and the twelfth valve 24 to remove dust carried out from the first modified adsorbent bed layer 9, and is used as a clean natural gas source through the fourteenth valve 28 and is supplied to users through the fifth gas source pipeline 31.
When the above process is performed, the fourth valve 11, the fifth valve 12, the seventh valve 14, the eighth valve 16, the ninth valve 18, the tenth valve 20, the eleventh valve 21, the thirteenth valve 27, and the fifteenth valve 29 are in the closed state, and the raw natural gas source is not passed through the second dry purification reaction vessel 15 by the second gas source pipeline 6.
When the first dry purification reaction vessel 10 is in an adsorption state for 8 hours and the first modified adsorbent bed 9 in the (reaction) vessel of the first dry purification reaction vessel 10 is saturated by adsorption, the first dry purification reaction vessel 10 is switched to an analysis state, the second dry purification reaction vessel 15 is switched to an adsorption state, and the raw material natural gas is 10000m3The gas source is a first gas source pipeline 1, enters a gravity separator 3 through a first valve 2 to remove impurities, enters a filtering separator 5 through a second valve (valve) 4 to be dehydrated, and a certain amount of acid impurities form a dry gas source without large-particle impurities, and passes through a second gas source pipeline 6, the natural gas source enters a second dry purification reaction vessel 15 through a second valve 7 and a seventh valve 14 through a second gas source pipeline 6, sulfides contained in the natural gas source in the second gas source pipeline 6 are removed through a second modified adsorbent bed layer 19, the desulfurized natural gas enters a dust filter 26 through a tenth valve 20 and a twelfth valve 24 to remove dust carried out from the second modified adsorbent bed layer 19, and the natural gas source is used as a clean natural gas source for users through a fourteenth valve 28 and a fifth gas source pipeline 31.
When the above process is performed, the third valve 8, the sixth valve 13, the sixth valve 16, and the ninth valve 18 are closed, and the remaining valves are opened, and the raw natural gas source does not pass through the first dry-type cleaning reaction vessel 10 through the second gas source pipe 6.
When the above process is performed, the first dry-type purification reaction vessel 10 is switched to the analysis state of 700m3H clean natural gas (total sulfide content is less than 20mg/m in terms of sulfur)3) The gas source enters the heat exchange device 25 through a sixth gas source pipeline 32 and a fifteenth valve 29, is heated to 250-350 ℃, passes through an eleventh valve (door) 21 and a fourth valve (door) 11, enters the saturated first dry type purification reaction vessel 10 (the adsorbent of the first modified adsorbent bed layer 9), is purged and penetrates through the first modified adsorbent bed layer 9 to ensure that the adsorbent bed layer is subjected to thermal desorption and regeneration, the saturated desorption gas source is discharged from a third gas source pipeline 17 through the bottom of the reaction vessel (the first dry type purification reaction vessel 10), passes through a fifth valve (door) 12, enters the conversion device 22 and passes through the bed layer of the hydrogenolysis conversion catalyst vessel 23, and the saturated desorption gas source is subjected to organic sulfur such as COS and CS in the third gas source pipeline 172The hydrogen in the third gas source pipeline 17 reacts with the natural gas analysis gas source through hydrogenolysis conversion to generate H2And S, the natural gas desorption gas after hydrogenolysis conversion passes through a tenth valve (door) 27 to form a converted saturated regenerated gas source, and the converted saturated regenerated gas source is conveyed to a desulfurization device of an oil and gas plant for treatment through a fourth gas source pipeline 30.
The analysis and regeneration process comprises four steps:
in the first step, 700m at 300 ℃ is used3H clean natural gas (total sulfide content is less than 20mg/m in terms of sulfur)3) Heating the saturated first modified adsorbent bed 9 and the first dry purification reactor vessel 10 for a total of 2.5 hours;
second, 100m at 300 ℃ is used3The temperature of the adsorbent bed (first modified adsorbent bed 9) was maintained for a total of 2.5 hours for clean natural gas;
thirdly, the heat exchange device 25 is closed, and 700m with the normal temperature of 35 ℃ is introduced into the first dry-type purification reaction vessel 103H clean natural gas, toCooling and purging the bed layer (the first modified adsorbent bed layer 9), wherein the process lasts for 2.5 hours;
and fourthly, stopping introducing the clean natural gas into the first dry type purification reaction vessel 10, allowing the bed layer (the first modified adsorbent bed layer 9) to stand for 0.5 hour, and after the regeneration process of 8 hours in total, returning the first dry type purification reaction vessel 10 to the initial state, wherein the modified adsorbent of the first modified adsorbent bed layer 9 is completely regenerated and can be put into an adsorption state for use.
The total length of the adsorption state is 8 hours, the total length of the analysis state is 8 hours, the first dry-type purification reaction vessel 10 and the second dry-type purification reaction vessel 15 are switched to work states every 8 hours, the two work states of adsorption and analysis are alternately carried out, and the time required by operating a system and a valve bank is 30 minutes during switching.
The modified adsorbent of the first modified adsorbent bed layer 9 and the second modified adsorbent bed layer 19 is based on one or more of 3A type molecular sieve, 4A type molecular sieve, 5A type molecular sieve, 13X type molecular sieve, coconut shell activated carbon and coal-based activated carbon, and is modified by one or more of alkali metal, alkali metal oxide, transition metal and transition metal oxide.
The catalyst of the catalyst container 23 for assisting the hydrogenolysis conversion of the saturated regeneration gas packed in the conversion apparatus 22 is an activated alumina-based catalyst, and one or more active materials such as Ni, Cu, Mo, Ti, Co, Ag, Fe, etc. are carried by impregnation or coating, and further, the catalyst is in a honeycomb body.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the utility model, and any modifications, equivalents and improvements made within the spirit and principle of the present invention are intended to be included within the scope of the present invention.
Claims (7)
1. The dry type natural gas purification device is characterized by comprising a gravity separator (3), a filtering separator (5) and a dry type purification reaction vessel which are sequentially arranged; the dry type purification reactor is characterized in that a modified adsorbent bed is arranged in the dry type purification reactor, the upper side of the dry type purification reactor is connected with a dust filter (26), the top of the dry type purification reactor is connected with a heat exchange device (25), the bottom of the dry type purification reactor is connected with a conversion device (22), a catalyst container (23) is arranged in the conversion device (22), and a plurality of dry type purification reactors are connected in parallel.
2. A dry purification apparatus for natural gas as claimed in claim 1, wherein 2 to 12 dry purification reaction vessels are provided in parallel.
3. A dry purification device for natural gas as claimed in claim 2, wherein valves are provided on the connecting pipes of the components of the device.
4. A dry purification apparatus for natural gas as claimed in claim 3, wherein said dry purification reaction vessel comprises 2 of a first dry purification reaction vessel (10) and a second dry purification reaction vessel (15) arranged in parallel, said first dry purification reaction vessel (10) is provided with a first modified adsorbent bed layer (9), and said second dry purification reaction vessel (15) is provided with a second modified adsorbent bed layer (19).
5. A dry purification device for natural gas as claimed in claim 4, wherein said first dry purification reaction vessel (10) is provided with a plurality of first modified adsorbent beds (9), and said second dry purification reaction vessel (15) is provided with a plurality of second modified adsorbent beds (19); when the dry type purification reaction vessel is in an adsorption state, natural gas raw gas enters the dry type purification reaction vessel and passes through the modified adsorbent bed from bottom to top; when the dry type purification reaction vessel is in a desorption state, the heated desorption gas source passes through the saturated modified adsorbent bed layer from top to bottom.
6. The dry purification device for natural gas as claimed in claim 5, wherein the dry purification reaction vessel contains a gas distribution device, the gas distribution device is a flow guide plate and is supported and fixed by ceramic ball packing.
7. The dry purification device for natural gas as claimed in claim 6, wherein the heat exchange device (25) is selected from one or more of a shell and tube heat exchanger, a plate heat exchanger, an electric heater and a heating furnace.
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