FULL TEMPERATURE RANGE SIMULATED ROTATED MOVING PRESSING SWING ADSORPTION (FTRSRMPSA) ENHANCED REACTION HYDROGEN GENERATION PROCESS FROM SHIFTED GAS

Abstract

Disclosed is a full temperature range simulated rotated moving pressure swing adsorption (FTrSRMPSA) enhanced reaction hydrogen generation process from a shifted gas. Multiple axial flow fixed bed adsorption reactors placed on a multi-channel rotary valve and ring-shaped rotary tray, and blended and loaded with medium and low-temperature shift catalysts and adsorbents are connected through a pipeline, and rotating directions and rotating speeds of the rotary valve and ring-shaped rotary tray are regulated. Therefore, gases complete mass and heat transfer of respective conversion reaction-adsorption and desorption regeneration steps by constantly coming in and going out of inlets and outlets of adsorption reactors to achieve a simulated rotated moving bed pressure swing adsorption enhanced reaction process. Hydrogen (H.sub.2) product gases are directly obtained therefrom, and have the purity and yield of greater than or equal to 99.9-99.99% and 92-95%, respectively. High purity carbon dioxide (CO.sub.2) is co-produced.

Claims

1. A full temperature range simulated rotated moving pressure swing adsorption (FTrSRMPSA) enhanced reaction hydrogen generation process from a shifted gas, wherein 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 2n10) adsorption reactors (towers) loaded with a medium-low temperature shift catalyst and a compound adsorbent blended in a certain proportion, having 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 (.sub.2, in second(s)/r), an m (a natural number in a range of 5m36)-channel rotary valve, placed at a center of the ring-shaped rotary try and rotating at a rotating speed (.sub.1, 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 (.sub.1 and .sub.2) thereof, a buffer tank, a condenser/or heat exchanger/or superheater/or pressurizer/or vacuum pump, wherein 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 comprise a shifted gas as a feed gas (F), an H.sub.2 product gas (H.sub.2PG), 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 comprising 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, comprising 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 (H.sub.2PG); a cyclic process of specific conversion reaction-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 (.sub.1) of the m-channel rotary valve and the rotating direction and the rotating speed (.sub.2) of the ring-shaped rotary tray, non-adsorbed phase gases flowing out from tops of the adsorption reactors (tower) just enter channels of the H.sub.2 product gas (H.sub.2PG) of the m-channel rotary valve through the process pipeline and flow out from the channel of the H.sub.2 product gas (H.sub.2PG) of the rotary valve to form the H.sub.2 product gas (H.sub.2PG) that enters the H.sub.2 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 CO.sub.2-enriched gas, or the desorption gas directly enters the condenser to remove a water and co-produce high concentration CO.sub.2, or enters a decarburization and H.sub.2 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 H.sub.2 product gas (H.sub.2PG) 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 (.sub.1) of the m-channel rotary valve and the rotating direction and the rotating speed (.sub.2) 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 (.sub.1) and the correspondingly rotating adsorption reactors (towers) on the ring-shaped rotary tray (.sub.2) 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 (.sub.1) of the m-channel rotary valve and the rotating direction and the rotating speed (.sub.2) 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 H.sub.2 product gas (H.sub.2PG) is obtained from the shifted gas, wherein 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%.

2. The full temperature range simulated rotated moving pressure swing adsorption (FTrSRMPSA) enhanced reaction hydrogen generation process from a shifted gas according to claim 1, wherein 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 (.sub.1 and .sub.2) comprises: 1) homodromous synchronizing, wherein the m-channel rotary valve and the ring-shaped rotary tray rotate homodromously in the clockwise or anticlockwise direction and .sub.1=.sub.20; 2) homodromous asynchronizing, wherein the m-channel rotary valve and the ring-shaped rotary tray rotate homodromously in the clockwise or anticlockwise direction and .sub.1>.sub.2 or .sub.1<.sub.2 or .sub.10/.sub.2=0 or .sub.1=0/.sub.20; 3) heterodromous synchronizing, wherein the m-channel rotary valve and the ring-shaped rotary tray rotate heterodromously in the clockwise/anticlockwise direction or anticlockwise/clockwise direction and .sub.1=.sub.2/0; and 4) heterodromous asynchronizing, wherein the m-channel rotary valve and the ring-shaped rotary tray rotate heterodromously in the clockwise/anticlockwise direction or anticlockwise/clockwise direction and .sub.1>.sub.2 or .sub.1<.sub.2 or .sub.10/.sub.2=0 or .sub.1=0/.sub.20, and preferably, in the homodromous rotation in the clockwise or anticlockwise direction in the homodromous synchronizing and homodromous asynchronizing, .sub.10/.sub.2=0 or .sub.1=0/.sub.20.

3. The full temperature range simulated rotated moving pressure swing adsorption (FTrSRMPSA) enhanced reaction hydrogen generation process from a shifted gas according to claim 1, wherein a combination of the closed cyclic operation step of conversion reaction-adsorption and desorption of the FTrSRMPSA-ERP system further comprises: 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 H.sub.2 and CO.sub.2 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 H.sub.2 product gas (H.sub.2PG) finally obtained is greater than or equal to 99.999%, and the product yield is greater than or equal to 95%.

4. The full temperature range simulated rotated moving pressure swing adsorption (FTrSRMPSA) enhanced reaction hydrogen generation process from a shifted gas according to claim 1, wherein the shifted gas (F) as a raw material is a mixed gas formed by 3060% of H.sub.2 (v), 10-20% CO (v), and 10-20% CO.sub.2 (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 Nm.sup.3/h.

5. The full temperature range simulated rotated moving pressure swing adsorption (FTrSRMPSA) enhanced reaction hydrogen generation process from a shifted gas according to claim 1, wherein the purge gas (P) is the pathwise pressure release gas (PP) inside the system or the H.sub.2 product gas (H.sub.2PG) 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 H.sub.2 product gas (H.sub.2PG) reaches 93% or above.

6. The full temperature range simulated rotated moving pressure swing adsorption (FTrSRMPSA) enhanced reaction hydrogen generation process from a shifted gas according to claim 1, wherein 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.

7. The full temperature range simulated rotated moving pressure swing adsorption (FTrSRMPSA) enhanced reaction hydrogen generation process from a shifted gas according to claim 1, wherein the final repressurization gas (FR) is the feed shifted gas (F) or the H.sub.2 product gas (H.sub.2PG) outside the system, and under a working condition that the purity of the H.sub.2 product gas (H.sub.2PG) is required to be greater than or equal to 99.99%, the H.sub.2 product gas (H.sub.2PG) is preferably used as the final repressurization gas (FR).

8. The full temperature range simulated rotated moving pressure swing adsorption (FTrSRMPSA) enhanced reaction hydrogen generation process from a shifted gas according to claim 1, wherein 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.

Description

BRIEF DESCRIPTION OF FIGURES

[0022] FIG. 1 is a flowchart of an embodiment 1 of the disclosure.

[0023] FIG. 2 is a flowchart of an embodiment 2 of the disclosure.

DETAILED DESCRIPTION

[0024] 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.

Embodiment 1

[0025] As shown in FIG. 1, a full temperature range simulated rotated moving pressure swing adsorption (FTrSRMPSA) enhanced reaction hydrogen generation process from a shifted gas is provided. A full temperature range simulated rotated moving bed is an FTrSRMPSA-ERP system which includes 4 axial flow fixed bed adsorption towers (n=4) with the height-diameter ratio of 2-3, loaded with blended catalysts/adsorbents formed by a ferric medium-temperature swing shift catalyst and lithium carbon molecular sieve/activated carbon mixed adsorbent stacked in a proportion of 1:1.2 at an interval, and placed on a ring-shaped rotary tray at the rotating speed of .sub.2=400-600 s; a corresponding driving mechanism; a 7-channel rotary valve at the rotating speed of .sub.1=400-600 s, having 7 channels (m=7) and placed at a center of the ring-shaped tray; a material pipeline where a material gas outside the 7-channel rotary valve and a system formed by an H.sub.2 product gas (H.sub.2PG), a feed gas (F), and a desorption gas (D) formed by a depressurization gas (D) and a purge waste gas (PW) comes in and goes out; a process pipeline connected from a built-in pipeline of the ring-shaped rotary tray to a position between the adsorption towers and an inlet and an outlet of the 7-channel rotary valve; and an H.sub.2 product gas (H.sub.2PG)/desorption gas (D) buffer tank, a compressor, a superheater, a heat exchanger 1/heat exchanger 2, a condenser, a steam boiler, and a CO.sub.2 adsorption tower. The rotating speed .sub.1 of the 7-channel rotary valve is equal to the rotating speed .sub.2 of the ring-shaped rotary tray (both are 400-600 s), and the rotating direction is the anticlockwise direction, i.e., the rotary regulation mode of the two is homodromous synchronization. 7 channels in the 7-channel rotary valve respectively have the following effects: 4 channels are material gas channels where the feed gas (F) (for example, m=1), the H.sub.2 product gas (H.sub.2PG) (for example, m=2), and the desorption gas (D) formed by the depressurization gas (D) (for example, m=5) and the purge waste gas (PW) (for example, m=6), and the feed gas (F) as the final repressurization gas (FR) (for example, m=7) circulate. 1 (for example, m=3) channel is process gas channel where the equalization drop gas (ED) and the equalization rise gas (ER) circulate. 1 (for example, m=4) channel is process flow channel where the pathwise pressure release gas (PP) as the purge gas (P) circulates. The compressor, the feed gas (F) buffer tank, and the superheater which are interconnected are sequentially arranged between the feed gas (F) material pipeline and the inlet end of the 7-channel rotary valve outside the system. The material pipeline where the desorption gas (D) formed by the depressurization gas (D) and the purge waste gas (PW) flows out from the outlet end of the 7-channel rotary valve is successively connected to the heat exchanger 2, the desorption gas (D) buffer tank, the condenser, the non-condensable gas 1 and CO.sub.2 adsorption tower, and the non-condensable gas 2 and feed gas (F) material pipeline. The condensate water is connected to the steam boiler, and the steam is connected to the heat exchanger 1 and the superheater. The material pipeline of the H.sub.2 product gas (H.sub.2PG) flowing out from the outlet end of the 7-channel rotary valve is connected to the H.sub.2 product gas (H.sub.2PG) buffer tank. The feed gas (F) is the hydrogen-containing shifted gas obtained by subjecting natural gas to steam catalytic reforming, with typical components of hydrogen (H.sub.2) with the concentration of 55% (v/v), carbon monoxide (CO) with the concentration of 15%, carbon dioxide (CO.sub.2) with the concentration of 5%, steam with the concentration of 15%, methane (CH.sub.4) with the concentration of 8%, and light hydrocarbon components with the concentration of 2%. The temperature of the shifted gas pressurized by the compressor to 0.6-0.8 MPa and overheated by the feed gas (F) buffer tank and the superheater is 120-130 C. The shifted gas enters the material channel (for example, m=1) of the feed gas (F) from a through hole material pipeline connected to the inlet end of the channel of the 7-channel rotary valve, enters the adsorption tower 1 through the process pipeline connected to the built-in pipeline of the ring-shaped rotary tray through the outlet of the through hole of the channel and connected to the inlet end of the adsorption tower 1, and is subjected to a conversion reaction adsorption (CR-A) step of a conversion reaction (CR) and an adsorption (A) reaction. A non-adsorbed phase gas flowing out from the outlet end of the adsorption tower 1 flows through the process pipeline connected to the adsorption tower 1, the built-in pipeline of the ring-shaped rotary tray, and the through hole of the material channel (for example, m=2) of the 7-channel rotary valve. The H.sub.2 product gas (H.sub.2PG) with the hydrogen (H.sub.2) purity greater than or equal to 99.99% (v/v) flowing out from the product gas (PG) material pipeline connected to the 7-channel rotary valve and the H.sub.2 product gas (H.sub.2PG) buffer tank enters the H.sub.2 product gas (H.sub.2PG) buffer tank and is directly delivered outside. After the CR-A step is finished, with homodromous synchronous rotation of the 7-channel rotary valve and the ring-shaped rotary tray in the anticlockwise direction, the adsorption tower 1 rotates to the position of the adsorption tower 2 in FIG. 1 for the equalization drop (ED) and pathwise pressure release (PP) operating steps. The equalization drop gas (ED) flowing out from the adsorption tower 1 flows through the built-in pipeline of the ring-shaped rotary tray, the equalization drop (ED) channel (for example, m=3) of the 7-channel rotary valve and the outlet end thereof, and the process pipeline where the built-in pipeline of the ring-shaped rotary tray is connected to the inlet end of the adsorption tower 4 just in the equalization rise (ER) step and enters the adsorption tower 4 (in this case, the position of the tower has stepped to the initial position of the adsorption tower 1) for pressure equalization till the pressures in the adsorption tower 1 and the adsorption tower 4 are equal (both are 0.2-0.3 MPa). Then, in the process that the ring-shaped rotary tray and the 7-channel rotary valve continue to rotate homodromously and synchronously, the adsorption tower 1 finishing the ED step enters the PP step, and the PP gas flowing out therefrom as the purge gas (P) flows through the built-in pipeline of the ring-shaped rotary tray and the PP channel (for example, m=4) of the 7-channel rotary valve and the outlet end thereof and the process pipeline where the built-in pipeline of the ring-shaped rotary tray is connected to the outlet end of the adsorption tower 3 just in the purge (P) step and enters the adsorption tower 3 (in this case, the position of the tower has stepped to the initial position of the adsorption tower 4) for purge (P). As the ring-shaped rotary tray and the 7-channel rotary valve continue to rotate homodromously and synchronously, the position of the adsorption tower 1 finishing the PP step moves to the initial position of the adsorption tower 3 in FIG. 1 for the depressurization (D) step. The depressurization gas (D) reversely dropped to normal pressure and flowing out from the adsorption tower 1 as the desorption gas (D) flows through the built-in pipeline of the ring-shaped rotary tray and the depressurization gas (D) channel (for example, m=5) of the 7-channel rotary valve and the outlet end thereof, is cooled by the heat exchanger 2 and flows through the desorption gas (D) buffer tank to enter the condenser. The non-condensable gas 1 generated from the condenser directly enters the CO2 adsorption tower taking an organic amine as the adsorbent for decarburization to generate a high concentration by-product CO.sub.2. The non-condensable gas 2 generated therefrom heated by heat exchange with the depressurization gas (D) in the heat exchanger 2 directly returns to the feed gas (F) to further recovery H.sub.2 and CO therein. The condensate generated by the condenser is water which enters the steam boiler to form steam, exchanges heat in the heat exchanger 1 and then enters the superheater, and together with the feed gas (F), forms a superheated feed gas which enters the FTrSRMPSA-ERP system. The proportion of the amount of circulating steam and the newly supplemented water (steam) can be adjusted according to a proportional requirement of H(H.sub.2O):C(CO) in the feed gas (F) in the conversion reaction, so that the conversion reaction and CO.sub.2 adsorption reach a complete dynamic balance. As the ring-shaped rotary tray and the 7-channel rotary valve continue to rotate homodromously and synchronously, the adsorption tower 1 finishing the D step enters the P step in the continuous moving process, the PP gas flowing out from the adsorption tower 4 just in the PP step as the purge gas (P) enters the adsorption tower 1 for purge (P), the purge waste gas (PW) generated therein flows through the built-in pipeline of the ring-shaped rotary tray and the PW channel (for example, m=6) of the 7-channel rotary valve and the outlet end thereof as the desorption gas (D), and the desorption gas cooled by the heat exchanger 2 flows through the desorption gas (D) buffer tank and is treated according to a treatment flow of the desorption gas (D). As the ring-shaped rotary tray and the 7-channel rotary valve further continue to rotate homodromously and synchronously, the position of the adsorption tower 1 finishing the P step moves to the initial position of the adsorption tower 4 in FIG. 1 to enter the ER and FR steps. The ED gas flowing out from the adsorption tower 3 just in the ED step flows through the built-in pipeline of the ring-shaped rotary tray and the ED/ER common channel (for example, m=3) of the 7-channel rotary valve and the outlet end thereof, flows out, and flows through the built-in pipeline of the ring-shaped rotary tray to enter the adsorption tower 1 for ER, so that the pressure in the adsorption tower 1 rises from normal pressure to be equal to the pressure in the adsorption tower 3 in the ED step (both are 0.2-0.3 MPa). As the ring-shaped rotary tray and the 7-channel rotary valve continue to rotate homodromously and synchronously, the adsorption tower 1 finishing the ER step receives the feed gas (F) outside the system as the FR gas which flows through the FR channel (for example, m=7) of the 7-channel rotary valve and inflates the inlets of the built-in pipeline of the ring-shaped rotary tray and the adsorption tower 1, so that the pressure in the adsorption tower 1 rises to the pressure (0.6-0.8 MPa) needed by the CR-A step, thereby forming the intact PSA enhanced reaction close-looped cyclic operation of the adsorption tower 1, i.e., the CR-A-ED/PP-D/P-ER/FR steps. Then, the adsorption tower 1 enters the next conversion reaction adsorption and desorption closed-loop cyclic operation process. The material gases and process gases correspondingly coming in and going out of the adsorption towers 2, 3, and 4 are also subjected to corresponding conversion reaction adsorption and desorption closed-loop cyclic operation steps in the conversion reaction adsorption and desorption closed-loop cyclic operation process of the adsorption tower 1 as the ring-shaped rotary tray and the 7-channel rotary valve continue to rotate homodromously and synchronously and the 7-channel rotary valve periodically and alternatively switches the 7 channels to synchronously switch the in-out positions of the material or process gases of the adsorption towers. The closed-loop cyclic operation steps of each adsorption tower correspond to those of the other 3 adsorption towers. Therefore, the high purity hydrogen (H.sub.2) product gas with the hydrogen purity greater than or equal to 99.99% is directly and continuously produced from the shifted gas having hydrogen (H.sub.2) with the concentration of 55% (v/v), carbon monoxide (CO) with the concentration of 15%, carbon dioxide (CO.sub.2) with the concentration of 5%, steam with the concentration of 15%, methane (CH.sub.4) with the concentration of 8%, and light hydrocarbon components with the concentration of 2% as the feed gas. The yield of the product gas is greater than or equal to 92%. Double heights of high purity and high yield of the simulated rotated PSA process based on the axial flow fixed bed of the SERP are achieved.

Embodiment 2

[0026] As shown in FIG. 2, based on embodiment 1, the shifted gas is the feed gas which is not pressurized by the compressor but is pressurized by a blower to 0.2 MPa or is 0.2 MPa shifted gas directly produced by the natural gas catalytic reforming reaction unit. The shifted gas enters the FTrSRMPSA-ERP system, a vacuumizing system where the outlet end of the adsorption tower and the vacuum pump are connected by an external pipeline is additionally arranged, and the CO.sub.2 adsorption tower is omitted. The rotating speed .sub.2 of the ring-shaped rotary tray in the system is adjusted to 0, i.e., the ring-shaped rotary tray does not rotate. The rotating direction of the 7-channel rotary valve remains the anticlockwise direction, and the rotating speed .sub.1 thereof is adjusted to 200-300 s. The initial positions of the 4 adsorption towers are consistent with that in embodiment 1 but are stationary. The 7-channel rotary valve rotates anticlockwise periodically (at a constant speed) to step and are switched periodically (at a constant speed) alternatively, so that each adsorption tower experiences the conversion reaction-adsorption and desorption closed-loop cyclic operation steps of conversion reaction-adsorption (CR-A)-depressurization (D)/vacuumizing (V)-vacuumizing purge (VP)-final repressurization (FR). The purge gas (P) is overheated steam under pressure outside the system at 140-150 C. Vacuumizing purge (VP) is performed after the adsorption tower is vacuumized and desorbed. The formed vacuumizing purge waste gas (VPW), together with, the depressurization gas (D) and the vacuumizing desorption gas (VD), serves as the desorption gas (D). The desorption gas subjected to heat exchange and cooling by the heat exchanger 2 enters the desorption gas (D) buffer tank and then enters the condenser for condensing. The generated condensate water subjected to heat exchange heating by the heat exchanger 1 and the H.sub.2 product gas (H.sub.2PG) enters the steam boiler. The formed steam, together with the feed gas, through the superheater enters the system for the closed-loop cyclic operation of conversion reaction-adsorption and desorption regeneration. 1 channel (for example, m=4) of the 7-channel rotary valve is an empty channel, which is used correspondingly in the vacuumizing step. All material gases and process gases are uniformly and alternatively distributed in 7 round channels in the rotary valve and the built-in pipeline in the ring-shaped rotary tray and the adsorption towers in the system, and the steps in the conversion reaction adsorption and desorption process are performed on PSA of one cyclic period simultaneously through the adsorption towers on the rotating rotary valve (.sub.1) and the connected ring-shaped rotary tray (.sub.2=0) which is correspondingly stationary. The positions of the process gases coming in and going out of the adsorption towers change constantly according to the rotating direction and rotating speed (.sub.1) of the 7-channel rotary valve, so that each adsorption tower can repeat the conversion reaction-adsorption and desorption step. Equivalently, each fixed bed adsorption tower without rotation completes respective conversion reaction-adsorption and desorption steps in the process that the 7-channel rotary valve rotates to further form the simulated rotated moving bed pressure swing adsorption enhanced reaction process. Therefore, the product H.sub.2 is obtained from the shifted gas containing H.sub.2/CO/CO.sub.2/H.sub.2O/CH.sub.4. The purity of the product is greater than or equal to 99.9%, and the yield thereof is greater than or equal to 92%.

[0027] 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.