CN212387734U - Pressure swing adsorption gas separation and purification hydrogen system - Google Patents
Pressure swing adsorption gas separation and purification hydrogen system Download PDFInfo
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- CN212387734U CN212387734U CN202020274107.6U CN202020274107U CN212387734U CN 212387734 U CN212387734 U CN 212387734U CN 202020274107 U CN202020274107 U CN 202020274107U CN 212387734 U CN212387734 U CN 212387734U
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Abstract
The utility model discloses a pressure swing adsorption gas separation purification hydrogen system solves the technical problem that prior art pressure swing adsorption gas separation efficiency is low and pressure swing adsorption gas separation system adsorption tower is bulky, the utility model discloses a 3 adsorption tower, 1 pans, 16 programme-controlled valves, 4 governing valves and corresponding feeding pipeline, product conveying pipeline, voltage-sharing pipeline, flushing pipe way and desorption pipeline. The feed gas is separated in 3 column 12 recycle steps to obtain a high purity product gas. The utility model discloses every adsorption tower is accomplished through 12 steps from absorption, voltage-sharing step down, reverse pressure, wash, the voltage-sharing cycle that steps up to product gas, and arbitrary adsorption tower all has an adsorption tower to be in the process that the feeding adsorbs and produce hydrogen constantly for raw material gas feeding and product gas production go on in succession. The circulation time is reduced from 480s to 396s at present, the feeding time of the adsorption tower is reduced, and therefore the volume of the adsorption tower is reduced, and the adsorption and separation efficiency of the system is improved.
Description
Technical Field
The utility model belongs to the technical field of pressure swing adsorption gas separation, concretely relates to pressure swing adsorption gas separation purification hydrogen system.
Background
The Pressure Swing Adsorption (PSA) gas separation technology is a gas separation technology that utilizes the difference in adsorption capacity of an adsorbent for different gases and the characteristic that the adsorption capacity increases with the increase of pressure and decreases with the decrease of pressure to perform adsorption at high pressure and desorption at low pressure, thereby realizing physical separation of gases. The pressure swing adsorption gas separation can realize high purity and high efficiency, so the method is widely applied to the fields of petrifaction, metallurgy, energy, environmental protection, medical treatment and the like.
The pressure swing adsorption gas separation can separate and purify various industrial gases such as hydrogen, oxygen, nitrogen, methane, carbon monoxide, carbon dioxide and the like from mixed gas, wherein the most widely applied technology is the pressure swing adsorption hydrogen purification technology.
The pressure swing adsorption method can be used for removing CO from hydrogen with the hydrogen content of more than 40 percent, such as shift gas, reformed gas, methanol cracking gas, methanol purge gas, refinery tail gas, synthetic ammonia tail gas and the like2、CO、CH4、 CnHm、N2、H2O and other impurities to obtain hydrogen with the purity of more than or equal to 99.9 percent, and meet various hydrogen requirements.
The pressure swing adsorption hydrogen extraction technology is continuously optimized in the application process, early patents such as US3430418 and US3456816 disclose 4-tower pressure swing adsorption process, along with the continuous increase of the pressure swing adsorption scale, the pressure is continuously increased to develop multi-tower pressure swing adsorption process technology, for example, CN1298410C discloses a pressure swing adsorption process with two sequential release tanks discloses a 10-tower process flow, and CN 103534002B discloses a process flow with more than 12 towers.
However, the pressure swing adsorption hydrogen extraction technology is not only applied to the large-scale industrial field, but also applied to the small and medium-scale field, so that the pressure swing adsorption process flow with less investment and higher efficiency needs to be developed. The way of saving investment and having high reliability is to reduce the number of adsorption towers and the number of program control valves, and patent CN1984705B discloses a continuous feed three-bed pressure swing adsorption system, which comprises 3 adsorption towers, 17 program control valves and 5 regulating valves, and realizes 12 process cycles as shown in the following table.
Wherein AD: adsorption and product production, ED 1: first equalization down, PPG: supply of purge gas, ED 2: second equalization down, BD: discharging; PG: receiving purified gas, EU 1: first equilibrium rise, EU 2: second equilibrium rise, PP: receiving product gas from the product manifold for product pressurization, and FD: the feed was pressurized.
As can be seen from the 12-step recycle table, the process has 3 adsorption feed steps and 1 feed pressurization step, i.e., 4 feed steps per sub-cycle, and can achieve the purpose of continuous feed, but the process has product hydrogen production only in the 3 adsorption steps, and the pressure in the adsorption column does not reach the adsorption pressure in the step where feed pressurization and second equilibrium lift are jointly performed, and no product gas is output, i.e., the flow path has 1/4 steps with no product gas output. In addition, the total cycle time of the 12-step cycle of the three-column flow of CN1984705B is 480s, i.e., the sub-cycle time is 160s, and the sub-cycle time is long, and the adsorption separation efficiency is not yet satisfactory.
Therefore, it is a technical problem to be solved by those skilled in the art to design a new three-tower pressure swing adsorption gas separation and purification system to improve the pressure swing adsorption gas separation efficiency of the system and reduce the volume of the system device.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is: the utility model provides a pressure swing adsorption gas separation purification hydrogen system, solves prior art pressure swing adsorption gas separation inefficiency and the big technical problem of adsorption tower volume.
In order to achieve the above object, the utility model adopts the following technical scheme:
a pressure swing adsorption gas separation and purification hydrogen system comprises a first adsorption tower, a second adsorption tower, a third adsorption tower, a middle tank, a feed gas conveying pipe, a pressure equalizing pipeline, a flushing pipeline, a gas desorption pipe and a product gas external conveying pipe, the feed gas conveying pipe is respectively connected with the first adsorption tower, the second adsorption tower and the third adsorption tower through pipelines, the desorption gas pipe is respectively connected with the first adsorption tower, the second adsorption tower and the third adsorption tower through pipelines, the product gas outward transmission pipe is respectively connected with the first adsorption tower, the second adsorption tower and the third adsorption tower through pipelines, the intermediate tank is respectively connected with the first adsorption tower, the second adsorption tower and the third adsorption tower through the pressure equalizing pipeline, the intermediate tank is respectively connected with the first adsorption tower, the second adsorption tower and the third adsorption tower through the flushing pipeline.
Further, a program control valve 1A is arranged on a pipeline connecting the feed gas conveying pipe and the first adsorption tower; preferably, a program control valve 1B is arranged on a pipeline connecting the feed gas conveying pipe and the second adsorption tower; more preferably, a program control valve 1C is arranged on a pipeline connecting the feed gas delivery pipe and the third adsorption tower.
Furthermore, a program control valve 3A is arranged on a pipeline connecting the air desorption pipe and the first adsorption tower; preferably, a program control valve 3B is arranged on a pipeline connecting the desorption pipe and the second adsorption tower; more preferably, a program control valve 3C is provided on a pipe connecting the desorption pipe and the third adsorption tower.
Furthermore, a program control valve 2A is arranged on a pipeline connecting the product gas outward transmission pipe and the first adsorption tower; preferably, a program control valve 2B is arranged on a pipeline connecting the product gas outward conveying pipe and the second adsorption tower; more preferably, a program control valve 2C is arranged on a pipeline connecting the product gas outward conveying pipe and the third adsorption tower.
Further, one end of the pressure equalizing pipeline is communicated with the intermediate tank, and the other end of the pressure equalizing pipeline is respectively communicated with the first adsorption tower, the second adsorption tower and the third adsorption tower through pipelines.
Furthermore, a program control valve 4A is arranged on a pipeline connecting the pressure equalizing pipeline and the first adsorption tower; preferably, a program control valve 4B is arranged on a pipeline connecting the pressure equalizing pipeline and the second adsorption tower; more preferably, a program control valve 4C is arranged on a pipeline connecting the pressure equalizing pipeline and the third adsorption tower.
Further, one end of the flushing pipeline is communicated with the intermediate tank, and the other end of the flushing pipeline is respectively communicated with the first adsorption tower, the second adsorption tower and the third adsorption tower through pipelines.
Furthermore, a program control valve 5A is arranged on a pipeline of the flushing pipeline connected with the first adsorption tower; preferably, a program control valve 5B is arranged on a pipeline connecting the flushing pipeline and the second adsorption tower; more preferably, a program control valve 5C is arranged on a pipeline connecting the flushing pipeline and the third adsorption tower.
Furthermore, an adjusting valve PV-1 is arranged on the product gas outward conveying pipe; preferably, the flushing pipeline is provided with a regulating valve PV-3; more preferably, the air release pipe is provided with a regulating valve PV-4; further preferably, a program control valve 4D is arranged on the pressure equalizing line.
Further, a final-rise pipeline is connected between the product gas outward conveying pipe and the pressure equalizing pipeline, and preferably, a regulating valve PV-2 is arranged on the final-rise pipeline.
Compared with the prior art, the utility model discloses following beneficial effect has:
the utility model has the advantages of simple structure and scientific and reasonable design, convenient to use, including 3 adsorption towers, 1 pans, 16 programme-controlled valves, 4 governing valves and corresponding inlet pipes, the product conveyer pipe, the pipeline of equalling the pressure, wash line and desorption pipe, with hydrogen content greater than 40%, pressure for the mixed feed gas purification of 0.8 ~ 3.0MPag to 99.9% above hydrogen, the adsorbent bed adopts compound adsorption bed, typical three-layer compound adsorption bed, follow supreme activated alumina that is respectively down in the adsorption bed, active carbon, and molecular sieve. Adopt 3 tower 12 circulation step flow, 16 programme-controlled valves and 4 governing valves, realize 2 steps of pressure-equalizing, every adsorption tower accomplishes from absorption, the pressure-equalizing step down, reverse pressure release, wash, the pressure-equalizing is boosted the circulation that rises to the product gas through 12 steps, any has an adsorption tower to be in the feeding and adsorbs and produce the hydrogen process constantly, make raw material gas feeding and product gas production go on in succession, and 12 steps of cycle process's sub cycle time reduces to 132s by traditional 160s, the total time of circulation reduces to 396s by present 480s, thereby promote system's separation purification efficiency, reduce the adsorption tower volume.
Drawings
FIG. 1 is a block diagram of the system structure of the pressure swing adsorption gas separation and purification hydrogen system of the present invention.
Fig. 2 is a schematic diagram of the tower 12-step circulation process of the utility model.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below with reference to the accompanying drawings. It is to be understood that the embodiments described are only some embodiments of the invention, and not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element referred to must have a specific orientation or be constructed and operated in a specific orientation, and thus, it should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; of course, mechanical connection and electrical connection are also possible; alternatively, they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood according to specific situations by those skilled in the art.
As shown in figure 1, the utility model provides a pair of pressure swing adsorption gas separation purification hydrogen system, including first adsorption tower, second adsorption tower, third adsorption tower, pans, feed gas conveyer pipe, pressure-equalizing line, flushing line, desorption mouth and product gas defeated outward pipe, feed gas conveyer pipe respectively with first adsorption tower second adsorption tower with third adsorption tower pipe connection, desorption gas pipe respectively with first adsorption tower second adsorption tower with third adsorption tower pipe connection, product gas defeated outward pipe respectively with first adsorption tower, second adsorption tower with third adsorption tower pipe connection, the pans pass through pressure-equalizing line respectively with first adsorption tower the second adsorption tower with the third adsorption tower pipe connection, the pans pass through flushing line respectively with first adsorption tower, The second adsorption tower is connected with the third adsorption tower.
The utility model is provided with a program control valve 1A on the pipeline connecting the feed gas conveying pipe and the first adsorption tower; preferably, a program control valve 1B is arranged on a pipeline connecting the feed gas conveying pipe and the second adsorption tower; more preferably, a program control valve 1C is arranged on a pipeline connecting the feed gas delivery pipe and the third adsorption tower. A program control valve 3A is arranged on a pipeline connecting the air desorption pipe and the first adsorption tower; preferably, a program control valve 3B is arranged on a pipeline connecting the desorption pipe and the second adsorption tower; more preferably, a program control valve 3C is provided on a pipe connecting the desorption pipe and the third adsorption tower. A program control valve 2A is arranged on a pipeline connecting the product gas outward conveying pipe and the first adsorption tower; preferably, a program control valve 2B is arranged on a pipeline connecting the product gas outward conveying pipe and the second adsorption tower; more preferably, a program control valve 2C is arranged on a pipeline connecting the product gas outward conveying pipe and the third adsorption tower.
One end of the pressure equalizing pipeline with the intermediate tank intercommunication, the other end pass through the pipeline respectively with first adsorption tower the second adsorption tower with the third adsorption tower intercommunication. A program control valve 4A is arranged on a pipeline connecting the pressure equalizing pipeline and the first adsorption tower; preferably, a program control valve 4B is arranged on a pipeline connecting the pressure equalizing pipeline and the second adsorption tower; more preferably, a program control valve 4C is arranged on a pipeline connecting the pressure equalizing pipeline and the third adsorption tower.
Flushing line's one end with the pans intercommunication, the other end pass through the pipeline respectively with first adsorption tower the second adsorption tower with the third adsorption tower intercommunication. A program control valve 5A is arranged on a pipeline for connecting the flushing pipeline and the first adsorption tower; preferably, a program control valve 5B is arranged on a pipeline connecting the flushing pipeline and the second adsorption tower; more preferably, a program control valve 5C is arranged on a pipeline connecting the flushing pipeline and the third adsorption tower.
The product gas outward conveying pipe of the utility model is provided with a regulating valve PV-1; preferably, the flushing pipeline is provided with a regulating valve PV-3; more preferably, the air release pipe is provided with a regulating valve PV-4; further preferably, a program control valve 4D is arranged on the pressure equalizing line. A final-rise pipeline is connected between the product gas outward conveying pipe and the pressure equalizing pipeline, and preferably, an adjusting valve PV-2 is arranged on the final-rise pipeline.
The utility model has the advantages of simple structure, design scientific and reasonable, convenient to use, including 3 adsorption towers, 1 pans, 16 programmable valve, 4 governing valves, and corresponding feed line, product conveying pipeline, voltage-sharing pipeline, flushing pipeline and desorption pipeline, with hydrogen content greater than 40%, pressure for 0.8 ~ 3.0 MPag's mixed feed gas purification to hydrogen more than 99.9%, the adsorbent bed adopts compound adsorption bed, typical three-layer compound adsorption bed, follow supreme active alumina that is respectively down in the adsorption bed, active carbon, and molecular sieve. Adopt 3 tower 12 circulation step flow, 16 programme-controlled valves and 4 governing valves, realize 2 steps of pressure-equalizing, every adsorption tower accomplishes from absorption, the pressure-equalizing step down, reverse pressure release, wash, the pressure-equalizing is boosted the circulation that rises to the product gas through 12 steps, any has an adsorption tower to be in the feeding and adsorbs and produce the hydrogen process constantly, make raw material gas feeding and product gas production go on in succession, and 12 steps of cycle process's sub cycle time reduces to 132s by traditional 160s, the total time of circulation reduces to 396s by present 480s, thereby promote system's separation purification efficiency, reduce the adsorption tower volume.
As shown in fig. 2, the utility model also provides a separation and purification method of pressure swing adsorption gas separation purification hydrogen system, adopts the twelve circulation preface of three towers to separate the feed gas in order to obtain high-purity product hydrogen, the twelve circulation preface includes four adsorption steps, two voltage-sharing step, one step of putting in reverse, two steps of washing, two voltage-sharing step and a product gas step of stepping up. In the two pressure equalizing and reducing steps, the first pressure equalizing and reducing step is to equalize the pressure of the adsorption tower and the intermediate tank; in the two pressure equalizing and boosting steps, the first pressure equalizing and boosting step is to equalize the pressure of the adsorption tower and the intermediate tank. The product gas is more than 99.9 percent of hydrogen; preferably, the pressure of the feed gas is 0.8-3.0 MPag; more preferably, the hydrogen content of the feed gas is greater than 40%.
The twelve cycle step sequence is specifically shown in the following table:
| step (ii) of | 1 | 2 | 3 | 4 | 5 | 6 | 7 | 8 | 9 | 10 | 11 | 12 |
| First adsorption tower | A1 | A2 | A3 | A4 | ED1 | ED2 | D | P | P | ER2 | ER1 | FR |
| Second adsorption tower | P | ER2 | ER1 | FR | A1 | A2 | A3 | A4 | ED1 | ED2 | D | P |
| Third adsorption tower | ED1 | ED2 | D | P | P | ER2 | ER1 | FR | A1 | A2 | A3 | A4 |
Wherein A1-A4: adsorption; ED 1: a first average pressure drop; ED 2: a second average pressure drop; d: reversely relieving pressure; p: flushing and regenerating; ER 2: second pressure equalization is increased; ER 1: first pressure equalization is increased; FR: and finally, boosting the pressure of the product gas.
The utility model discloses step 1 is 30s, and step 2 is 12s, and step 3 is 30s, and step 4 is 60s, and step 5 is 30s, and step 6 is 12s, and step 7 is 30s, and step 8 is 60s, and step 9 is 30s, and step 10 is 12s, and step 11 is 30s, and step 12 is 60 s.
The utility model discloses a 3 adsorption towers, 1 pans, 16 programme-controlled valves, 4 governing valves, the raw materials trachea, the product trachea, the pressure-equalizing gas pipeline, wash the trachea line, and decompose the breathing pipe, after hydrogen-containing feed gas gets into 3 towers pressure swing adsorption purification hydrogen systems, reach the hydrogen more than 99.9% after the absorption of composite adsorption bed, every adsorption tower is in proper order through adsorbing, the pressure-equalizing step down, put in reverse, wash, the pressure-equalizing is stepped up, step such as product gas steps, every circulation is 12 steps, 12 steps include 4 adsorption step, 2 pressure-equalizing step down, 1 is put in reverse step, 2 washing step, 2 pressure-equalizing step up, and 1 product gas step up, the flushing gas derives from the gas of the first pressure drop in the pans, the step of putting in the same direction in the conventional adsorption pressure swing technology is saved. The pressure of the feed gas is 0.8-3.0 MPag; the hydrogen content of the feed gas is more than 40%. The sub-cycle time of the 12-step circulation process is 132s, the total circulation time is 396s, the adsorption separation and purification efficiency is high, and the volume of the whole system adsorption tower is small. 1-4 adsorbents are filled in the adsorption tower, preferably 3 adsorbents, wherein the 3 adsorbents are respectively activated alumina, activated carbon and a molecular sieve, and the activated alumina, the activated carbon and the molecular sieve are distributed in the adsorption bed from bottom to top.
In the adsorption step of the utility model, the adsorption tower opens the No. 1 valve (No. 1 valve is 1A, 1B or 1C, the following No. 2 valve, No. 3 valve, No. 4 valve and No. 5 valve are the same) and the No. 2 valve (No. 2 valve is 2A, 2B or 2C), the hydrogen-containing feed gas enters the adsorption tower through the raw material gas pipeline and the No. 1 valve, the impurities are adsorbed by the composite adsorbent adsorption bed, and the purified product hydrogen is transported out through the No. 2 valve, PV-1 and the product gas export pipeline; after 4 continuous adsorption steps, closing the valve No. 1 and the valve No. 2, opening the valve No. 4 and the valve No. 4D, equalizing the pressure of the adsorption tower and the intermediate tank, and equalizing the pressure of the adsorption tower and the pressure of the intermediate tank; then, closing the 4D valve, opening a No. 4 valve corresponding to the adsorption tower in the second pressure equalizing step, equalizing the pressure of the two adsorption towers, and finishing the second pressure equalizing step by the adsorption towers; closing the No. 4 valve, opening the No. 3 valve and the PV-4 regulating valve, allowing the gas in the adsorption tower to flow out of the hydrogen purification system through the No. 3 valve, the PV-4 valve and the desorption gas pipeline system, further reducing the pressure of the adsorption tower to a lower regeneration pressure, and preliminarily desorbing the impurities adsorbed by the adsorbent in the adsorption tower; after the reverse pressure reduction is finished, opening a No. 5 valve and a PV-3 valve, allowing the hydrogen in the intermediate tank to enter an adsorption tower through a regulating valve PV-3, the No. 5 valve and a flushing gas pipeline, performing reverse flushing regeneration on an adsorption bed, and allowing the regenerated desorption gas to flow out of a hydrogen purification system through the No. 3 valve, the PV-4 and a desorption gas pipeline; after 2 continuous washing steps, the adsorption bed is thoroughly regenerated; the regenerated adsorption tower closes the valve No. 3 and the valve No. 5 and PV-3 and PV-4, opens the valve No. 4, and is communicated with the adsorption tower in the second pressure equalizing and reducing step, and then carries out the second pressure equalizing and reducing step; after the second equalizing step is finished, opening a 4D valve, and communicating with the middle tank to perform the first equalizing step; and after the first step of uniform rising is completed, closing the No. 4 valve and the No. 4D valve, opening the No. 5 valve and the PV-2 valve, and finally boosting the pressure of the adsorption tower by using the product hydrogen. One adsorption tower completes 12 steps in one cycle, and 3 adsorption towers and 1 intermediate tank are coupled to complete continuous hydrogen purifying process and adsorbent regenerating process.
The utility model discloses 12 steps of pressure swing adsorption purification hydrogen systems in 3 towers can realize that hydrogen content is more than 40%, and pressure is at the gaseous high-efficient separation of the hydrogenous of 0.8 ~ 3.0MPag, and the cycle period that contains 2 voltage-sharing steps is 396 s.
The utility model discloses be greater than 40% with hydrogen content, the mixed feed gas purification that pressure is 0.8 ~ 3.0MPag is to hydrogen more than 99.9%, and the adsorbent bed adopts compound adsorption bed, and typical three-layer compound adsorption bed follows supreme activated alumina, active carbon and the molecular sieve of being respectively down in the adsorption bed. As shown in fig. 1, each adsorption tower is connected with 5 program control valves, and 16 program control valves in total, wherein 1 valve (1 valve includes 1A, 1B and 1C, and the following 2 valves, 3 valves, 4 valves and 5 valves are the same) is a raw material gas valve, 2 valve is a product gas valve, 3 valve is a desorption gas valve, 4 valve is a pressure equalizing valve, and 5 valve is a flushing valve; in addition, 4 regulating valves are provided, and PV-1 is a product gas pressure regulating valve for controlling the product gas pressure to be stable; PV-2 is a final boost regulating valve for controlling the boost speed; PV-3 is a flushing regulating valve for controlling the flow rate of flushing gas; PV-4 is desorption gas regulating valve for controlling gas flow rate in the reverse discharge process. The twelve-cycle step sequence of the utility model is detailed in the following 12-step flow time sequence chart:
12-step flow time sequence chart
| Step (ii) of | 1 | 2 | 3 | 4 | 5 | 6 | 7 | 8 | 9 | 10 | 11 | 12 |
| Step time/s | 30 | 12 | 30 | 60 | 30 | 12 | 30 | 60 | 30 | 12 | 30 | 60 |
| First adsorption tower | A1 | A2 | A3 | A4 | ED1 | ED2 | D | P | P | ER2 | ER1 | FR |
| Second adsorption tower | P | ER2 | ER1 | FR | A1 | A2 | A3 | A4 | ED1 | ED2 | D | P |
| Third adsorption tower | ED1 | ED2 | D | P | P | ER2 | ER1 | FR | A1 | A2 | A3 | A4 |
Wherein A1-A4: adsorption; ED 1: a first average pressure drop; ED 2: a second average pressure drop; d: reversely relieving pressure; p: flushing and regenerating; ER 2: second pressure equalization is increased; ER 1: first pressure equalization is increased; FR: and finally, boosting the pressure of the product gas.
The utility model discloses a complete 3 tower 12 steps circulation process as follows:
step 1: the first adsorption tower is in the adsorption step, a valve 1A and a valve 2A which are connected with the first adsorption tower are opened, other valves are closed, the raw gas enters the first adsorption tower through the valve 1A, the raw gas flows out of the top of the adsorption tower after passing through the composite adsorption bed, the product hydrogen with the purity of 99.9 percent flows out of the top of the adsorption tower, and the product gas is sent out of the device after being stabilized by the valve 2A and the PV-1; the second adsorption tower is in a flushing step, a 5B valve and a 3B valve which are connected with the second adsorption tower are in an open state, other valves are in a closed state, gas in the middle tank enters the adsorption tower from the top of the adsorption tower through a regulating valve PV-3, a flushing pipeline and the 5B valve to flush and regenerate the adsorption bed, and regenerated waste gas is sent out of a boundary area through the 3B valve and a desorption pipeline; and the third adsorption tower is in the first pressure equalizing step, namely the 4C valve connected with the third adsorption tower is in an open state, other valves are in a closed state, the 4D valve connected with the intermediate tank is in an open state, and the third adsorption tower and the intermediate tank are in pressure equalizing. During step 1, PV-4 is in an on state.
Step 2: the first adsorption tower still maintains the adsorption state in the step 1; the second adsorption tower is in the second pressure equalizing step, and the third adsorption tower is in the second pressure equalizing step; namely closing the 5B valve and the 3B valve of the second adsorption tower and PV-3, closing the 4D valve, opening the 4B valve, communicating the second adsorption tower with the third adsorption tower, and carrying out pressure balance; in step 2, PV-4 is in an off state;
and step 3: the first adsorption tower still maintains the adsorption state in the step 2; the second adsorption tower is in the first pressure equalizing step, and the third adsorption tower is in the reverse releasing step; namely closing the 4C valve of the third adsorption tower, opening the 4D valve, communicating the second adsorption tower with the intermediate tank, and carrying out pressure balance on the second adsorption tower and the intermediate tank; the pressure of the second adsorption tower is increased, and the pressure of the intermediate tank is reduced; and opening a 3C valve and a PV-4 valve of the third adsorption tower, reversely sending the gas of the third adsorption tower out of the device through the 3C valve and the PV-4 valve, gradually reducing the pressure of the third adsorption tower to the normal pressure, and gradually desorbing the adsorbed impurities in the third adsorption tower.
And 4, step 4: the first adsorption tower still maintains the adsorption state in the step 3; the second adsorption tower is in the final pressure boosting step of the product gas, and the third adsorption tower is in the flushing step; closing the 4D valve, opening the PV-2, and boosting the pressure of the second adsorption tower by using the product gas until the pressure of the second adsorption tower is raised to the adsorption pressure; and opening a 5C valve and a PV-3 of the third adsorption tower, introducing gas in the buffer tank into the third adsorption tower through the PV-3 and the 5C, flushing and regenerating the adsorption tower, and delivering regenerated waste gas out of the battery limit zone through a regulating valve PV-4. In step 4, PV-4 is in an on state;
and 5: the first adsorption tower is converted into a first pressure equalizing step from the adsorption step, a valve 1A and a valve 2A of the first adsorption tower are closed, a valve 4A and a valve 4D are opened, a valve 4B is closed, the first adsorption tower is communicated with the intermediate tank, the first adsorption tower and the intermediate tank are equalized in pressure, the pressure of the first adsorption tower is reduced, and the pressure of the intermediate tank is increased; the second adsorption tower is in the adsorption step, PV-2 is closed, a valve 1B and a valve 2B of the second adsorption tower are opened, the feed gas enters the second adsorption tower through the valve 1B, the product hydrogen with the purity of 99.9 percent flows out of the top of the adsorption tower after passing through the composite adsorption bed, and the product gas is sent out of the device after being stabilized by the valve 2B and PV 1; the third adsorption tower still keeps a flushing step, namely, the gas in the intermediate tank enters the third adsorption tower through PV-3 and 5C to flush and regenerate the adsorption bed, and the regeneration waste gas flows out of the device through a 3C valve and PV-4. In step 5, PV-4 is in an on state;
step 6: the second adsorption tower continuously keeps the adsorption step, the first adsorption tower is in the second pressure equalizing step, and the third adsorption tower is in the second pressure equalizing step; closing the 4D valve, the 5C valve, the 3C valve and the PV-3, opening the 4C valve, communicating the first adsorption tower with the third adsorption tower, balancing the pressure of the two adsorption towers, reducing the pressure of the first adsorption tower, and increasing the pressure of the third adsorption tower; at step 6, PV-4 is in an off state.
And 7: the second adsorption tower continuously keeps the adsorption step, the first adsorption tower is in the reverse releasing step, the 4A valve is closed, the 3A valve and the PV-4 valve are opened, the first adsorption tower carries out reverse pressure release, the gas in the adsorption tower reversely flows out of the adsorption tower, the pressure of the adsorption tower is correspondingly reduced, the impurities adsorbed by the adsorption bed are partially desorbed, and the desorbed gas flows out of the device through the PV-4 valve; and the third adsorption tower is in the first pressure equalization rising step, the 4D valve is opened, the second adsorption tower is communicated with the intermediate tank, the third adsorption tower and the intermediate tank are subjected to pressure balance, the pressure of the third adsorption tower rises, and the pressure of the intermediate tank is reduced.
And 8: the second adsorption tower continues to maintain the adsorption step; the first adsorption tower is in a flushing step, a valve 5A and a valve PV-3 are opened, gas in the intermediate tank enters the first adsorption tower through the valve PV-3 and the valve 5A, the adsorption bed is flushed and regenerated, and desorption gas flows out of the device through the valve 3A and the valve PV-4; and the third adsorption tower is in a final pressure boosting step, the 4D valve is closed, the PV-2 is opened, the third adsorption tower is subjected to final pressure boosting by using product gas, the pressure of the third adsorption tower is gradually boosted to the adsorption pressure, and the pressure boosting speed is controlled by the PV-2.
And step 9: continuously keeping the first adsorption tower in the flushing step, enabling gas in the intermediate tank to enter the first adsorption tower through the PV-3 and 5A valves, flushing and regenerating the adsorption bed, and enabling desorption gas to flow out of the device through the 3A valve and the PV-4 valve; the third adsorption tower is shifted to an adsorption step, a 4C valve and a PV-2 valve are closed, a 1C valve and a 2C valve are opened, the feed gas enters the third adsorption tower through the 1C valve, the product hydrogen with the purity of 99.9 percent flows out of the top of the adsorption tower after passing through a composite adsorption bed, and the product gas is sent out of the device after being stabilized by the 2C valve and the PV 1; and the second adsorption tower is in the first pressure equalizing step, the valve 1B and the valve 2B are closed, the valve 4B and the valve 4D are opened, the second adsorption tower is communicated with the intermediate tank, the pressure equalization is carried out on the second adsorption tower and the intermediate tank, the pressure of the second adsorption tower is reduced, and the pressure of the intermediate tank is increased.
Step 10: the third adsorption tower continues to maintain the adsorption step; the first adsorption tower is in the second pressure equalizing step, and the second adsorption tower is in the second pressure equalizing step; closing the 3A valve, the 5A valve, the 4D valve and the PV-3 valve, opening the 4A valve, communicating the first adsorption tower with the second adsorption tower, equalizing the pressure of the two adsorption towers, increasing the pressure of the first adsorption tower, and decreasing the pressure of the second adsorption tower;
step 11: the third adsorption tower continues to maintain the adsorption step; the first adsorption tower is in the first pressure equalizing step, and the second adsorption tower is in the reverse releasing step; closing the 4B valve, opening the 4D valve, communicating the first adsorption tower with the intermediate tank, equalizing the pressure of the first adsorption tower with the intermediate tank, increasing the pressure of the first adsorption tower, and decreasing the pressure of the intermediate tank; and opening the 3B valve and the PV-4, reversely decompressing the second adsorption tower, reducing the pressure of the second adsorption tower, desorbing part of impurities adsorbed by the adsorption bed, allowing desorbed gas to flow out of the device through the PV-4, and controlling the pressure reduction speed of the second adsorption tower through the PV-4.
Step 12: the third adsorption tower continues to maintain the adsorption step; the first adsorption tower is in the step of boosting the pressure of the product gas, and the second adsorption tower is in the step of flushing; closing the 4D valve, opening the PV-2, performing final pressure boosting on the first adsorption tower by using product gas, gradually boosting the pressure of the first adsorption tower to the adsorption pressure, and controlling the pressure boosting speed by the PV-2; and opening the valve 5B and the valve PV-3, introducing the gas in the intermediate tank into a second adsorption tower through the valve PV-3 and the valve 5B, flushing and regenerating the adsorption bed, and discharging the desorption gas out of the device through the valve 3B and the valve PV-4, wherein one cycle is finished.
As shown in fig. 2, a: adsorption; ED 1: a first average pressure drop; ED 2: a second average pressure drop; d: releasing pressure in the reverse direction; p: flushing; ER 2: second pressure equalization is increased; ER 1: first pressure equalization is increased; FR: finally boosting the pressure; RP: boosting the pressure; DP: and (5) reducing the pressure.
The utility model discloses in the 12 steps pressure swing adsorption processes in 3 towers, every adsorption tower is accomplished through 12 steps from absorption, voltage-sharing step-down, reverse pressure, wash, the voltage-sharing cycle that steps up to product gas, and any one all has an adsorption tower to be in the feeding and adsorbs and produce the hydrogen process constantly for raw material gas feeding and product gas production go on in succession. In the 3-tower 12-step circulation process, the step integration is adopted, so that the circulation time of the 3-tower process is reduced from 480s to 396s at present, the feeding time of the adsorption tower is reduced, the volume of the adsorption tower is reduced, and the adsorption and separation efficiency of the system is improved.
Finally, it should be noted that: the above embodiments are only preferred embodiments of the present invention to illustrate the technical solution of the present invention, but not to limit the same, and certainly not to limit the scope of the present invention; although the present invention has been described in detail with reference to the foregoing embodiments, it should be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention; that is, the technical problems solved by the present invention are still consistent with the present invention, and all the modifications or colors made in the spirit and the idea of the main design of the present invention are included in the protection scope of the present invention; in addition, will the technical scheme of the utility model direct or indirect application is in other relevant technical field, all including on the same reason the utility model discloses an in the patent protection scope.
Claims (24)
1. The utility model provides a pressure swing adsorption gas separation purification hydrogen system, its characterized in that includes first adsorption tower, second adsorption tower, third adsorption tower, intermediate tank, feed gas conveyer pipe, pressure equalizing line, flushing line, desorption pipe and product gas defeated outward pipe, feed gas conveyer pipe respectively with first adsorption tower the second adsorption tower with third adsorption tower pipe connection, desorption gas pipe respectively with first adsorption tower the second adsorption tower with third adsorption tower pipe connection, product gas defeated outward pipe respectively with first adsorption tower, the second adsorption tower with third adsorption tower pipe connection, the intermediate tank passes through pressure equalizing line respectively with first adsorption tower the second adsorption tower with the third adsorption tower is connected, the intermediate tank pass through flushing line respectively with first adsorption tower, The second adsorption tower is connected with the third adsorption tower.
2. The pressure swing adsorption gas separation and purification hydrogen system of claim 1, wherein a program control valve 1A is arranged on a pipeline connecting the feed gas conveying pipe and the first adsorption tower.
3. The pressure swing adsorption gas separation and purification hydrogen system of claim 2, wherein a program control valve 1B is arranged on a pipeline connecting the feed gas conveying pipe and the second adsorption tower.
4. The pressure swing adsorption gas separation and purification hydrogen system of claim 2, wherein a program control valve 1C is arranged on a pipeline connecting the feed gas conveying pipe and the third adsorption tower.
5. The system of claim 1, wherein a programmable valve 3A is arranged on a pipeline connecting the desorption pipe and the first adsorption tower.
6. The system of claim 5, wherein the pipeline connecting the desorption pipe and the second adsorption tower is provided with a program control valve 3B.
7. The system of claim 5, wherein a program control valve 3C is disposed on a pipeline connecting the desorption pipe and the third adsorption tower.
8. The pressure swing adsorption gas separation and purification hydrogen system of claim 1, wherein a program control valve 2A is arranged on a pipeline connecting the product gas outward conveying pipe and the first adsorption tower.
9. The pressure swing adsorption gas separation and purification hydrogen system of claim 8, wherein a program control valve 2B is arranged on a pipeline connecting the product gas outgoing pipe and the second adsorption tower.
10. The pressure swing adsorption gas separation and purification hydrogen system of claim 8, wherein a program control valve 2C is arranged on a pipeline connecting the product gas outgoing pipe and the third adsorption tower.
11. The pressure swing adsorption gas separation and purification hydrogen system as claimed in claim 1, wherein one end of the pressure equalizing pipeline is communicated with the intermediate tank, and the other end is communicated with the first adsorption tower, the second adsorption tower and the third adsorption tower respectively through pipelines.
12. The pressure swing adsorption gas separation and purification hydrogen system of claim 11, wherein a program control valve 4A is arranged on a pipeline connecting the pressure equalizing pipeline and the first adsorption tower.
13. The pressure swing adsorption gas separation and purification hydrogen system of claim 12, wherein a program control valve 4B is arranged on a pipeline connecting the pressure equalizing pipeline and the second adsorption tower.
14. The pressure swing adsorption gas separation and purification hydrogen system of claim 12, wherein a program control valve 4C is arranged on a pipeline connecting the pressure equalizing pipeline and the third adsorption tower.
15. The pressure swing adsorption gas separation and purification hydrogen system as claimed in claim 1, wherein one end of the flushing line is communicated with the intermediate tank, and the other end is communicated with the first adsorption tower, the second adsorption tower and the third adsorption tower respectively through pipelines.
16. The pressure swing adsorption gas separation and purification hydrogen system of claim 15, wherein a program control valve 5A is arranged on a pipeline connecting the flushing pipeline and the first adsorption tower.
17. The pressure swing adsorption gas separation and purification hydrogen system of claim 16, wherein a program control valve 5B is arranged on a pipeline connecting the flushing pipeline and the second adsorption tower.
18. The pressure swing adsorption gas separation and purification hydrogen system of claim 16, wherein a program control valve 5C is provided on a pipe connecting the flushing line and the third adsorption tower.
19. The pressure swing adsorption gas separation and purification hydrogen system of claim 1, wherein the product gas export line is provided with a regulating valve PV-1.
20. The pressure swing adsorption gas separation and purification hydrogen system of claim 19, wherein the flushing line is provided with a regulating valve PV-3.
21. The system of claim 19, wherein the desorption tube is provided with a regulating valve PV-4.
22. The pressure swing adsorption gas separation and purification hydrogen system of claim 19, wherein the pressure equalizing line is provided with a program control valve 4D.
23. The pressure swing adsorption gas separation and purification hydrogen system of claim 1, wherein a final-rise pipeline is connected between the product gas export pipeline and the pressure equalizing pipeline.
24. The system of claim 23, wherein the final pipeline has a regulating valve PV-2.
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