Patent Application
20250083955
The disclosure relates to the field of hydrogen (H2) generation by hydrocarbon reforming, and in particular to a full temperature range simulated rotated moving pressure swing adsorption (FTRSRMPSA) enhanced reaction hydrogen generation process from a shifted gas.
The shifted gas mainly refers to a mixed gas formed by impure compositions such as 30-60% of H2 (volume ratio, similar in the following), 10-20% of CO, 10-20% of CO2, unreacted water, hydrocarbons, other hydrocarbons and organic matter byproducts generated by catalytically reforming oxides from light hydrocarbon mixtures, alcohols and the like and steam at certain temperature and pressure and under the action of a reforming catalyst. CO and water are further subjected to a medium or low-temperature shift reaction at certain temperature and pressure and under the action of a shift catalyst to generate H2 and CO2, and then H2 and CO2 are then subjected to organic amine absorption or pressure swing adsorption (PSA) decarburization and PSA H2 purification step to obtain a high purity H2 product. Most typical light hydrocarbon raw material catalytic reforming hydrogen generation processes include: performing a reforming reaction first to generate a shifted gas; then subjecting the shifted gas to a shift reaction to generate a shifted gas rich in H2 and CO2; and then subjecting H2 and CO2 to an organic amine adsorption or PSA decarburization and PSA purification step to finally obtain the H2 product. Although the hydrogen generation processes are mature, they have the shortcomings of long flow, large occupied area, high energy consumption and high equipment investment and cost. Therefore, the processes are technically transformed and updated at home and abroad, so that the flow is further simplified, and the occupied area and cost are reduced.
A method is to develop a dual functional composite catalyst and a matched integrated reactor and process. The core is to integrate the catalytic reforming reaction and the shift reaction in one reactor. This method has been applied to industrialized devices. For example, in a methanol-to-hydrogen process, because the catalytic reforming (cracking) reaction temperature and pressure of methanol steam are comparatively mild, most used catalysts are copper catalysts, the reaction temperature and pressure of which are equivalent to those of the catalyst based on ferric catalysts in the shift reaction. The heat balance processes of the two reactions are relatively close, so that the effect of achieving a dual functional catalyst is relatively ideal. The used catalysts in the catalytic reforming reaction process of methane and the like are high-temperature catalysts such as nickel catalysts. The reaction temperature is usually 700-900° C., which is far higher than the reaction temperature 100-300° C. needed by the medium and low temperature shift catalyst, resulting in substantial increase of the development difficulty of the dual functional catalyst.
Another method is a Sorption Enhanced Reaction Process (SERP for short) first invented by Air Products and Chemicals Inc (APCI), where a catalyst needed by reaction and an adsorbent needed by adsorption separation fill a same vessel, so that a reactor and an adsorber are integrated to form a sorption enhanced reactor which organically couples a chemical reaction with an adsorption separation process, which is completely different from the chemical reaction and adsorption separation respectively performed in two independent vessels: the reactor and the adsorber. The fundamental principle of the SER is to use the Le Chatelier thermodynamic principle, that is, when the system is (chemically) balanced, if any condition such as concentration, temperature and pressure of a balanced state is changed, the balance moves toward the direction where its change can be weakened. With respect to the catalytic reforming reaction and shift reaction system for generating H2 by a reforming reaction of light hydrocarbon steam, when the concentrations of the reactants and products are in a state invariant with time, i.e., the system reaches the chemical (reaction) balance. If an adsorbent that selectively adsorbs the product CO2 is added into the reaction system, the product CO2 will be adsorbed immediately during the reaction, thereby breaking through the chemical balance. The reaction will proceed to the direction facilitating generation of H2, so that the reaction approaches to completion. The sorption enhanced reaction process has the advantages that the reaction conversion ratio of the product yield or purity can be improved by improving the operating conditions, and the energy consumption and cost can be lowered by simplifying the process. The SERP developed by APCI first for pressure swing regeneration of hydrogen supply for fuel cells is used for methane steam conversion hydrogen generation. The used adsorbent is a high-temperature and water-resistant reversible chemical adsorbent (K2CO3-hydrotalcite) for selective adsorptive removal of CO2 in a reaction region with the reaction temperature of 400-550° C. The adsorbed and saturated adsorbent is regenerated by the PSA cycle, a shift catalyst with a nickel active component loaded on aluminum oxide and the CO2 chemical adsorbent fill the pressure swing adsorption enhanced reactor in a mixed manner to form the PSA enhanced reaction process of two axial flow fixed beds. One adsorption reactor is used to perform the conversion reaction-adsorption step and the other one is to perform the desorption-regeneration step of reverse pressure drop, vacuumizing purge, and reverse pressure rise. The operating pressure of the conversion reaction-adsorption step is 70-350 kPa. With respect to normal pressure depressurization and vacuumizing purge, the purge gas is 5-10% H2 steam. The desorption gas containing H2, methane (CH4), CO2, and water is condensed to remove water and is outputted as a fuel gas. The pressurized gas is the feed gas of a methane and steam mixed gas, and the purity of the H2 product obtained is 94.4%. The content of CH4 is 5.6%, that of CO2 is 40 ppmv, that of CO is 30 ppmv, and the methane conversion ratio reaches up to 73%, which is much higher than the conversion ratio 50-55% of the shifted gas prepared by the conventional catalytic conversion and shifting reaction two-step method experienced by steam methane catalytic reforming (SMR). The H2 concentration in the shifted gas is increased, the load of subsequent PSA hydrogen purification is also reduced, and moreover, the hydrogen generation flow is simplified, and the investment and equipment and operation costs are lowered. However, the SERP developed by APCI has some obvious shortcomings: first, the process cannot product the H2 product with higher purity directly, and further PSA hydrogen purification is still needed to obtain high purity H2; second, the selected adsorbent is comparatively special, needs to be high-temperature and water-resistant, and a common commercial adsorbent is hardly used; third, the reaction temperature is too high: even the nickel catalyst in the SERP of APCI matching a CO2 removing adsorbent can be decreased to about 500° C., which is much lower than 700-900° C. needed by a catalytic reforming nickel catalyst in a conventional two-section reaction and the energy consumption is less, however, it is unfavorable for the pressure swing adsorption process of CO2 at higher temperature, and under low pressure adsorption, CO2 is likely to be adsorbed and unsaturated to escape and enter the non-adsorbed phase gas, so that the CO2 exceeds the standard severely in the shifted gas; fourth, PSA in the SERP actually only adsorbs at the lower temperature: desorption regeneration includes: performing normal pressure depressurization first, where the obtained depressurization gas as the feed gas returns to the other adsorption reactor in the conversion reaction-adsorption step, and reversely purging the bed with steam that contains 5-10% H2 with the temperature lower than the reaction temperature, the obtained purge waste gas is condensed to remove water and is then taken as the fuel gas, so that the yield of H2 has a certain loss; moreover, the used adsorbent is the chemical adsorbent, which is the consumptive adsorbent that is high in consumption and cannot be cyclically used like the conventional adsorbent; moreover, the thermal stability of the adsorbent itself will be greatly affected as a result of the temperature difference stress in the adsorption and desorption regeneration process at the higher temperature and steam content; and fifth, as the height-diameter ratio of the adsorption reactor in the SERP system is relatively less, it is quite unfavorable for the diffusion path of CO2. Therefore, the SERP of methane steam reforming hydrogen generation by APCI hardly replaces the conventional SMR process. Therefore, APCI has developed another “temperature swing sorption enhanced reaction” process (TSSER) using temperature swing adsorption for water gas (shifted gas) hydrogen generation. As the ferric catalyst in the shifting reaction is relatively low in acting temperature, the temperature in the conversion reaction-adsorption step is 300-400° C., which is lower than 400-550° C. of the SERP, facilitating adsorption of CO2. Therefore, the purity of the produced H2 is further improved. However, the desorption regeneration temperature of the adsorbent reaches 500-550° C., the adsorbent will be greatly affected by the temperature difference stress in the adsorption and desorption regeneration process at higher temperature and steam content, the negative influence generated on the thermal stability of the adsorbent itself is higher than that of the SERP, and therefore, the replacing frequency of the adsorbent in the TSSER process is higher than that of the SERP, resulting in corresponding increase of the cost.
Regardless of the SERP or TSSER process, its critical technology is selection of the adsorbent and its corresponding process. Because the methane catalytic reforming reaction and the shifting reaction are high in speed and the endothermic and exothermic processes of the reactions themselves are different, the thermodynamic and dynamic adsorption rates of CO2 will also be affected greatly, which further results in whether the conversion reaction-adsorption step is completed at the same time to change the chemical reaction balance moving all the way toward a direction favorable for H2 generation. Thus, APCI has to use temperature and water-resistant chemical adsorbent with extremely high adsorption rate to match movement of the conversion reaction-adsorption balance system with the cost of short service life, high cost of the adsorbent and low purity of the H2 product and yield. Other factors that affect the adsorption efficiency are neglected, such as air flow distribution, CO2 adsorption mass transfer path, selection of the adsorbent and catalyst and corresponding filling mode or solid shape of the adsorbent/catalyst itself, adsorption and desorption cyclic operation mode and the like.
To overcome some problems in the previous existing adsorption enhanced reaction process in raw material (including methane or methanol) and steam catalytic reforming/conversion hydrogen generation process, the disclosure provides a novel process of full temperature range simulated rotated moving PSA (FTrSRMPSA) for CO2 removal and H2 purification by a pressure swing adsorption enhanced reaction of a shifted gas. In the process, based on the pressure swing adsorption enhanced reaction process (PSA-ERP), multiple axial flow fixed bed adsorption reactors placed at a center of a multi-channel rotary valve, placed on a ring-shaped rotary tray around the multi-channel rotary valve, and blended and loaded with medium and low-temperature shift catalysts and adsorbents are connected through a pipeline, and a rotating direction and a rotating speed (ω1) of the rotary valve and a rotating direction and a rotating speed (ω2) of the ring-shaped rotary tray are regulated by making full use of temperature and pressure of the shifted gas, properties of the medium-low temperature shift catalyst/adsorbent, the temperature range (90-150° C.) of components H2 and CO2 of the product, the adsorption separation coefficient within the pressure range of 0.2-1.0 MPa, and the difference on physical and chemical properties. Therefore, gases flowing through the channels of the rotary valve, the pipelines where the inlets and outlets of the channels of the rotary valve and the inlets and outlets of the adsorption reactors on the ring-shaped rotary tray are connected, and the adsorption reaction beds rotatably moving in the adsorption towers complete mass and heat transfer of respective conversion reaction-adsorption and desorption regeneration steps by constantly coming in and going out of positions of inlets and outlets of the adsorption reactors with rotation of the adsorption reaction beds, so that the shifted gas reaction balance tends to move toward a complete reaction direction therewith to further form a “simulated rotated moving bed” PSA enhanced reaction process, which achieves the simulated rotated moving bed pressure swing adsorption enhanced reaction process based on axial flow fixed bed pressure swing adsorption. The process is suitable for working conditions where corresponding flow, component concentration, pressure or temperature of the shifted gas fluctuate while achieving “double heights” of yield and purity and avoiding deep adsorption, makes full use of various advantages of the axial flow fixed bed pressure swing adsorption and related art including fixed bed pressure swing sorption enhanced reaction (SERP), fixed bed pressure swing sorption enhanced reaction (TSSER), rotated wheel adsorption and simulated moving bed, and overcomes defects in the existing technical processes. A specific solution of the process is as follows:
A full temperature range simulated rotated moving pressure swing adsorption (FTrSRMPSA) enhanced reaction hydrogen generation process from a shifted gas is provided, where the full temperature range simulated rotated moving pressure swing adsorption enhanced reaction process (FTrSRMPSA-ERP) system is formed by n (a natural number in a range of 2≤n≤10) adsorption reactors (towers) loaded with a medium-low temperature shift catalyst and a compound adsorbent blended in a certain proportion, having an axial flow fixed bed adsorption reactors (towers) with a certain height-diameter ratio and placed on a ring-shaped rotary tray at a rotating speed (ω2, in second(s)/r), an m (a natural number in a range of 5≤m≤36)-channel rotary valve, placed at a center of the ring-shaped rotary try and rotating at a rotating speed (ω1, in second(s)/r), a material pipeline where material gases outside the rotary valve and a system come in and go out, a process pipeline connected from a built-in pipeline of the ring-shaped tray to a position between the adsorption reactors (towers) and the rotary valve, and a driving mechanism correspondingly driving the ring-shaped rotary tray and the rotary valve in rotating directions and regulating rotating speeds (ω1 and ω2) thereof, a buffer tank, a condenser/or heat exchanger/or superheater/or pressurizer/or vacuum pump, where the pipeline connecting inlets and outlets of the adsorption reactors (towers) and an inlet and an outlet of the m-channel rotary valve is connected to the built-in pipeline pre-arranged in the ring-shaped rotary tray to form the process pipeline and has the same number m as that of the channels of the rotary valve; positions of the material gas coming in and going out of the FTrSRMPSA-ERP system are fixed by distributing the rotary channels of the m-channel rotary valve, the material gases thereof include a shifted gas as a feed gas (F), an H2 product gas (H2PG), a purge gas (P) outside the system, a final repressurization gas (FR) outside the system, and a desorption gas (D) formed by a depressurization gas (D) or/and a vacuumizing gas (V) or/and a purge waste gas (PW) and are correspondingly connected to devices including the buffer tank, condenser/or heat exchanger/or superheater/or pressurizer/or vacuum pump; the position where the process gases flow in the process pipeline connected through the built-in pipeline in the ring-shaped rotary tray between the inlet and outlet of the m-channel rotary valve and the inlets and outlets of the adsorption reactors (towers) changes alternately in a mobile manner;
the process gases flow in the FTrSRMPSA-ERP system, including the feed gas (F), a pathwise pressure release gas (PP), the purge gases (P) inside and outside the system, an equalization drop gas (ED), the desorption gas (D) formed by the depressurization gas (D) or/and the vacuumizing gas (V) or/and the purge waste gas (PW), an equalization rise gas (ER), the final repressurization gas (FR), and the product hydrogen (H2PG); a cyclic process of specific adsorption and desorption is as follows: the feed shifted gas (F) outside the FTrSRMPSA-ERP system enters feed gas (F) inlets of the multi-channel rotary valve, and enters a conversion reaction-adsorption (CR-A) step from bottoms of the adsorption reactors (towers) through the process pipeline connected to the feed gas (F) channels and the outlet of the rotary valve, the built-in pipeline of the ring-shaped rotary tray, and corresponding inlets of the one or more axial flow fixed adsorption reactors (towers) in a conversion reaction-adsorption (CR-A) state on the ring-shaped rotary tray; as continuously stepped in a matched manner by regulating the rotating direction and the rotating speed (ω1) of the m-channel rotary valve and the rotating direction and the rotating speed (ω2) of the ring-shaped rotary tray, non-adsorbed phase gases flowing out from tops of the adsorption reactors (tower) just enter channels of the H2 product gas (H2PG) of the m-channel rotary valve through the process pipeline and flow out from the channel of the H2 product gas (H2PG) of the rotary valve to form the H2 product gas (H2PG) that enters the H2 product gas buffer tank and is then outputted; after the conversion reaction-adsorption (CR-A) step is completed by the adsorption reactors (towers) in the conversion reaction-adsorption (CR-A) state, as the m-channel rotary valve and the ring-shaped rotary tray rotate continuously to step, and/or the adsorption reactors (towers) after the conversion reaction-adsorption (CR-A) perform a pathwise pressure release (PP) or equalization drop (ED) step on one or more adsorption reactors (towers) in a purge (P) or equalization rise (ER) state through the process pipeline inside the system; the adsorption reactors (towers) after the pathwise pressure release (PP) or equalization drop (ED) step enter a depressurization (D) or/and vacuumizing (V) or/and purge (P) step as the m-channel rotary valves and the ring-shaped rotary tray rotate continuously to step; the desorption gas (D) formed by the depressurization gas (D) or/and vacuumizing gas (V) or/and purge waste gas (PW) flowing out from the adsorption towers flow out through the built-in pipeline or an external pipeline of the ring-shaped rotary tray and depressurization gas (D)/vacuumizing gas (V)/purge waste gas (PW) channel of the rotary valve and the outlet end thereof and flow through the desorption gas (D) buffer tank, and the desorption gas (D) is a CO2-enriched gas, or the desorption gas directly enters the condenser to remove a water and co-produce high concentration CO2, or enters a decarburization and H2 recovery step, or returns to a natural gas/light hydrocarbon steam reforming reaction to a step of preparing the shifted gas or feed gas as carbon-hydrogen ratio adjustment; the adsorption reactor (tower) after the depressurization (D) or/and vacuumizing (V) or/and purge (P) step enters an equalization rise (ER) or waiting area (-) step as the m-channel rotary valve and the ring-shaped rotary ring rotate continuously to step; the process gases flow out from the adsorption reactor (tower) in the ED step and enter the adsorption reactor (tower) in the ER step through the built-in pipeline of the ring-shaped rotary tray and the ED channel of the rotary valve for equalization, so that the adsorption reactor (tower) in the ER or/and waiting area (-) step is finished till the pressure of the adsorption reactor (tower) in the ER step is equal to the pressure in the adsorption reactor (tower) in the ED step, and enters a final repressurization (FR) step as the m-channel rotary valve and the ring-shaped rotary ring rotate continuously to step; the H2 product gas (H2PG) or the feed shifted gas (F), as the final repressurization gas (FR), flow through the FR channels of the m-channel rotary valves and the built-in pipeline of the ring-shaped rotary tray to enter the adsorption reactors (towers) for pressure inflation till the pressure in the adsorption reactor (tower) reaches the conversion reaction-adsorption pressure needed by the CR-A step, and a cyclic operation of conversion reaction-adsorption and desorption next round is prepared; each adsorption reactor (tower) performs one or more step and each step and is matched by regulating the rotating direction and the rotating speed (ω1) of the m-channel rotary valve and the rotating direction and the rotating speed (ω2) of the ring-shaped rotary tray, so that the m channels in the rotating m-channel rotary valve are connected to time scales in the cyclic operation of conversion reaction-adsorption and desorption of the n rotating adsorption reactors (towers) in the ring-shaped rotary tray end to end to form a circle, and integrally form operating cyclicity of the conversion reaction-adsorption and desorption process of the PSA enhanced reaction; all material gases and process gases are uniformly and alternately distributed in m round (slotted) channels in the m-channel rotary valve and the built-in pipeline in the ring-shaped rotary tray and the adsorption reactors (towers) in the system, in the PSA enhanced reaction process of one cyclic period, the steps in the conversion reaction-adsorption and desorption process are simultaneously performed on the adsorption reactors (towers) on the rotating m-channel rotary valve (ω1) and the correspondingly rotating adsorption reactors (towers) on the ring-shaped rotary tray (ω2) connected, respectively; the positions of the process gases coming in and going out of the adsorption reactors (towers) change constantly by matching the rotating direction and the rotating speed (ω1) of the m-channel rotary valve and the rotating direction and the rotating speed (ω2) of the ring-shaped rotary tray, so that each adsorption reactor (tower) repeats the conversion reaction-adsorption and desorption step, and equivalently, each fixed bed adsorption reactor (tower) completes respective conversion reaction-adsorption and desorption step while the m-channel rotary valve and the ring-shaped rotary tray rotate, so as to form “a simulated rotated moving bed” PSA enhanced reaction process; and therefore, the product H2 product gas (H2PG) is obtained from the shifted gas, where the purity of the gas product is greater than or equal to 99.99%, and the yield thereof is greater than or equal to 92%.
Further, the full temperature range simulated rotated moving pressure swing adsorption (FTrSRMPSA) enhanced reaction hydrogen generation process from a shifted gas is provided, where the step of regulating and matching the rotating directions of the m-channel rotary valve and the ring-shaped rotary tray and the rotating speeds thereof (ω1 and ω2) includes: 1) homodromous synchronizing, where the m-channel rotary valve and the ring-shaped rotary tray rotate homodromously in the clockwise or anticlockwise direction and ω1=ω2/≠0; 2) homodromous asynchronizing, where the m-channel rotary valve and the ring-shaped rotary tray rotate homodromously in the clockwise or anticlockwise direction and ω1>ω2 or ω1<ω2 or ω1≠0/ω2=0 or ω1=0/ω2≠0; 3) heterodromous synchronizing, where the m-channel rotary valve and the ring-shaped rotary tray rotate heterodromously in the clockwise/anticlockwise direction or anticlockwise/clockwise direction and ω1=ω2/≠0; and 4) heterodromous asynchronizing, where the m-channel rotary valve and the ring-shaped rotary tray rotate heterodromously in the clockwise/anticlockwise direction or anticlockwise/clockwise direction and ω1>ω2 or ω1<ω2 or ω1≠0/ω2=0 or ω1=0/ω2≠0, and preferably, in the homodromous rotation in the clockwise or anticlockwise direction in the homodromous synchronizing and homodromous asynchronizing, ω1≠0/ω2=0 or ω1=0/ω2≠0.
Even further, the full temperature range simulated rotated moving pressure swing adsorption (FTrSRMPSA) enhanced reaction hydrogen generation process from a shifted gas is provided, where a combination of the closed cyclic operation step of conversion reaction-adsorption and desorption of the FTrSRMPSA-ERP system further includes: 1-2 time pressure equalization, 1-2 batch purge, 1 time vacuumizing, 1-2 time variable temperature pressure swing adsorption of heating and cooled heat exchanging, 1 time mutual dislocation of pathwise pressure release and equalization drop, and 1 waiting area step; moreover, the number (n) of the adsorption reactors (towers) and the number (m) of the corresponding m-channel rotary valve are increased, the height (radius)-diameter ratio (h/r) of the adsorption towers is decreased, and the rotating speeds of the m-channel rotary valve and the ring-shaped rotary tray are enough high in speed or enough short in rotating period, a separation effect of products H2 and CO2 in a shifted gas adsorption enhanced reaction system infinitely approaches a “steady” mass transfer separation process of the moving bed, the shifted gas reaction balance tends to move toward a complete reaction direction therewith, and the purity of the H2 product gas (H2PG) finally obtained is greater than or equal to 99.999%, and the product yield is greater than or equal to 95%.
Even further, the full temperature range simulated rotated moving pressure swing adsorption (FTrSRMPSA) enhanced reaction hydrogen generation process from a shifted gas is provided, where the shifted gas (F) as a raw material is a mixed gas formed by 30-60% of H2 (v), 10-20% CO (v), and 10-20% CO2 (v) obtained by catalytically reforming or thermally cracking methane or methanol or other hydrocarbons by steam, unreacted water, hydrocarbons and other hydrocarbons or organic matter byproduct impurities, and the temperature of the shifted gas is 90-150° C., the pressure thereof is 0.2-1.0 MPa, and the flow thereof is 100-20000 Nm3/h.
Even further, the full temperature range simulated rotated moving pressure swing adsorption (FTrSRMPSA) enhanced reaction hydrogen generation process from a shifted gas is provided, where the purge gas (P) is the pathwise pressure release gas (PP) inside the system or the H2 product gas (H2PG) outside the system, and is purged in batches through one or more holes in the channels (slots) of the m-channel rotary valve, at most 4 holes are formed, the pathwise pressure release gas (PP) inside the system is preferably taken as the purge gas (P), and the yield of the H2 product gas (H2PG) reaches 93% or above.
Even further, the full temperature range simulated rotated moving pressure swing adsorption (FTrSRMPSA) enhanced reaction hydrogen generation process from a shifted gas is provided, where in the depressurization (D) step, desorption is performed in a vacuumizing manner; the additionally arranged vacuum pump is connected to a material flow pipeline of the m-channel rotary valve where the desorption gas flows out or is directly connected to the external pipeline connected to the outlet end of the adsorption tower on the ring-shaped rotary tray, and a control valve is arranged on the external pipeline, and preferably, the vacuum pump is directly connected to the external pipeline connected to the outlet end of the adsorption tower on the ring-shaped rotary tray and the control valve is arranged on the external pipeline.
Even further, the full temperature range simulated rotated moving pressure swing adsorption (FTrSRMPSA) enhanced reaction hydrogen generation process from a shifted gas is provided, where the final repressurization gas (FR) is the feed shifted gas (F) or the H2 product gas (H2PG) outside the system, and under a working condition that the purity of the H2 product gas (H2PG) is required to be greater than or equal to 99.99%, the H2 product gas (H2PG) is preferably used as the final repressurization gas (FR).
Even further, the full temperature range simulated rotated moving pressure swing adsorption (FTrSRMPSA) enhanced reaction process from a shifted gas is provided, where the n loaded blended catalysts/adsorbents in the FTrSRMPSA-ERP system are formed by stacking ferric medium shift catalysts and lithium-carbon molecular sieves/activated carbon particles in a proportion of 1:(1-1.5) at an interval, or composite catalytic adsorbent particles of ferric active component loading carbon nanotubes (CNTs) or carbon fibers (CNFs)/activated carbon (AC)/aluminum oxide, or cellular and bundled regular composite catalytic adsorbents formed by high polymer organic matters or carbon nanotubes or carbon fibers or formed by loading ferric active components by taking silicate as a base material, and preferably, the catalysts/adsorbents are formed by stacking ferric medium shift catalysts and lithium-carbon molecular sieves/activated carbon particles in a proportion of 1:1.1 at an interval or the bundled and cellular regular composite adsorbents formed by high polymer organic matters or carbon nanotubes or carbon fibers or formed by loading ferric/lithium active components by taking silicate (containing silicon fluoride, ceramics, and glass fibers) as the base material.
The disclosure has the following beneficial effects:
In order to make persons skilled in the art better understand the solutions of the disclosure, the technical solutions in the embodiments of the disclosure will be described clearly and completely below in conjunction with drawings.
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Apparently, the embodiments described above are merely some, rather than, all of the embodiments of the disclosure. Based on the embodiments recorded in the disclosure, all other embodiments obtained by persons skilled in the art without making creative efforts or structural changes made under enlightenment of the disclosure with same or similar technical solutions of the disclosure shall fall within the protection scope of the disclosure.
| Number | Date | Country | Kind |
|---|---|---|---|
| 202210260623.7 | Mar 2022 | CN | national |
| Number | Date | Country | |
|---|---|---|---|
| Parent | PCT/CN2022/130759 | Nov 2022 | WO |
| Child | 18810675 | US |
