CN210303031U - Multi-bed temperature swing adsorption gas purification system - Google Patents
Multi-bed temperature swing adsorption gas purification system Download PDFInfo
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- CN210303031U CN210303031U CN201920519184.0U CN201920519184U CN210303031U CN 210303031 U CN210303031 U CN 210303031U CN 201920519184 U CN201920519184 U CN 201920519184U CN 210303031 U CN210303031 U CN 210303031U
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Abstract
The utility model provides a gas purification system with multi-bed temperature swing adsorption, which belongs to the technical field of gas purification. The system comprises at least three adsorption beds, each adsorption bed is provided with a feeding end and a discharging end, a raw material pipeline and an exhaust pipeline are connected with the feeding ends of the adsorption beds, a gas collecting pipeline is connected with the discharging ends of the adsorption beds, a heating pipeline is connected with the feeding ends and the discharging ends of the adsorption beds, and a heater is arranged on the heating pipeline. The raw material gas enters each adsorption bed through a raw material pipeline, and each adsorption bed repeatedly performs the circulation of the adsorption step, the heating step, the precooling step and the cooling step. The utility model discloses can reduce temperature swing adsorption gas purification system's waste heat discharge and improve its product gas recovery rate, have energy-conserving meaning of great in industrial occasions such as air drying and natural gas treatment.
Description
Technical Field
The utility model relates to a gas purification technology field especially indicates a gas purification system is adsorbed to multi-bed temperature swing.
Background
The gas purification process is a common raw material gas treatment process in the fields of metallurgy, energy, chemical industry, environmental protection and the like, such as gas pollutant removal, compressed air drying, raw material natural gas drying and the like, and mainly aims to remove impurities (water vapor, carbon dioxide, acetylene, nitrogen dioxide, carbon monoxide, hydrogen sulfide, volatile organic compounds and the like) in raw material gas to a trace level to obtain product gas with the purity reaching the standard, so that the hazards of environmental pollution, pipeline freezing and blockage, material corrosion, explosion and the like caused by the impurities are avoided, and the smooth proceeding of subsequent use or working procedures is ensured.
The temperature swing adsorption process is a commonly used gas purification process that is carried out by an adsorbent bed having a feed end and a discharge end, the adsorbent bed being filled with an adsorbent of a specified thickness. The purification principle of the temperature swing adsorption process is as follows: in the working mode, the raw gas is continuously introduced into the adsorption bed to adsorb impurities and change into product gas, the introduction of the raw gas is stopped after the preset time, and the adsorption bed is switched to the regeneration mode to be regenerated so as to be repeatedly used, so that the adsorption bed alternately operates in the working mode and the regeneration mode. In order to continuously obtain the product gas, two adsorption beds are generally connected in parallel in a conventional temperature swing adsorption gas purification system for switching use (see fig. 1).
In the operation mode, the adsorption bed mainly goes through one step: and an adsorption step, namely introducing the feed gas into the feed end of the adsorption bed so as to carry out gas-solid contact, and after selectively adsorbing impurities in the feed gas by using an adsorbent, obtaining a product gas without impurities from the discharge end of the adsorption bed. Common adsorbents include molecular sieves, alumina, silica gel, activated carbon, and the like. The adsorption process has a heat effect, and heat is released during adsorption, and heat is required to be absorbed during desorption. The adsorption capacity of the adsorbent decreases with increasing temperature, and therefore, in order to secure the adsorption capacity of the adsorbent, the adsorption process is generally performed at normal temperature. During the adsorption process, a concentration front of impurities is formed in the adsorbent bed, and the front is continuously pushed forward along the flowing direction of the raw material gas. When the point of turnover or a predetermined time has been reached, the adsorbent bed or adsorbent needs to be regenerated for reuse, i.e. the adsorbent bed is switched to regeneration mode.
In the regeneration mode, the adsorbent bed undergoes steps including a heating step, a cooling step, and other steps. The main steps are a heating step and a cooling step, and in addition to this, the adsorption bed may be subjected to other steps, as required, such as: a pressurization step and a depressurization step for changing the pressure inside the adsorption bed, and since the adsorption bed needs to be adsorbed at a high pressure but regenerated at a normal pressure in some cases, the depressurization operation is performed before the regeneration and the pressurization is performed before the adsorption. In the heating step, the adsorbent is heated so as to desorb the impurities adsorbed by the adsorbent; in the cooling step, the adsorbent is cooled to restore its adsorption capacity.
The heating and cooling steps are realized by introducing the regeneration gas with different temperatures into the adsorption bed, namely the regeneration gas is introduced into the discharge end of the adsorption bed along the direction opposite to the flowing direction of the raw material gas. The regeneration gas is usually free of impurities, and generally comes from the product gas of the adsorption bed, and because the product gas is obtained by consuming energy, the consumption of the regeneration gas should be reduced to reduce the loss of the product gas, so as to improve the product gas recovery rate of the system. In addition, in order to reduce the energy consumption of the system, the heat input should be saved as much as possible, for example, a "heat pulse" method is generally adopted to regenerate the adsorption bed, that is, the heating is finished and the cooling is started before the whole adsorption bed (all the adsorbents) is heated to the regeneration temperature.
In the heating step based on the regeneration of the 'heat pulse' method, the regeneration gas at normal temperature is heated by a heater to the regeneration temperature, and then is introduced into the adsorption bed, when the high-temperature regeneration gas passes through the bed layer, on one hand, the heat is brought to the adsorbent for heating and desorbing the adsorbate, and on the other hand, the desorbed impurities are brought out of the adsorption bed. The regeneration temperatures employed for the different adsorbents vary, but are generally between 50 ℃ and 300 ℃. With the continuous introduction of high-temperature regeneration gas, a heating temperature front is formed in the bed layer, and the heating temperature front can be continuously pushed forward along the circulation direction of the regeneration gas. At the end of the heating step, the heating temperature front advances to a position in the middle of the bed.
In the cooling step based on regeneration of the thermal pulse method, unheated normal-temperature regeneration gas is directly introduced into the adsorption bed, and when the normal-temperature regeneration gas passes through the bed layer, on one hand, the adsorbent near the discharge end is cooled, the stored heat is brought to the position near the feed end to heat the adsorbent, and on the other hand, desorbed impurities are continuously brought out of the adsorption bed. With the continuous introduction of the normal-temperature regeneration gas, a cooling temperature front edge is formed in the bed layer, and the cooling temperature front edge and the heating temperature front edge jointly form a forward-propelled thermal pulse. Over time, the "heat pulse" advances forward until it penetrates the bed, and as it traverses the bed, heat is continually used to desorb the adsorbate, causing its peak temperature to gradually decrease. To ensure effective regeneration of the entire adsorbent bed, the peak temperature of the "hot pulse" as it penetrates the bed, i.e., the cold blow peak, must be greater than some minimum temperature requirement (e.g., activated alumina adsorbents typically require a cold blow peak greater than 100 ℃). During the "heat pulse" breakthrough, some of the impurities in the adsorbent bed are being desorbed, and therefore, the gas exiting the adsorbent bed during the cooling step carries residual heat along with the desorbed impurities. The residual heat quantity is considerable, and generally accounts for about 20-60% of the total regenerative heating energy consumption. In the conventional temperature swing adsorption gas purification system, since only two adsorption beds are switched to be used, namely one adsorption bed is regenerated while the other adsorption bed is adsorbing, the waste heat can only be directly discharged because the waste heat has no suitable use place. Because the heating energy consumption required by the regeneration of the adsorption bed is huge, the method for recycling the waste heat discharged by the adsorption bed in the cooling step has important energy-saving significance.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is to provide a gas purification system is adsorbed to multi-bed temperature swing.
The system comprises a plurality of adsorption beds and pipelines, wherein each adsorption bed comprises a feeding end and a discharging end, each pipeline comprises a raw material pipeline, an exhaust pipeline, a gas collecting pipeline and a heating pipeline, the raw material pipeline and the exhaust pipeline are connected with the feeding ends of the adsorption beds, the gas collecting pipeline is connected with the discharging ends of the adsorption beds, the heating pipelines are connected with the feeding ends and the discharging ends of the adsorption beds, and heaters are arranged on the heating pipelines.
A feed line for selectively providing a feed gas; a gas collection line for selectively delivering a product gas; a gas discharge line for selectively discharging gas from each adsorption bed; a heating line for selectively transferring gas between the adsorption beds; and the heater is used for heating the gas.
Wherein, the adsorption bed is one of a horizontal axial flow adsorption bed, a vertical axial flow adsorption bed or a vertical radial flow adsorption bed, the number of the adsorption beds is not less than three, and at least one layer of adsorbent is filled in the adsorption bed.
The adsorbent is at least one of molecular sieve, alumina, silica gel, active carbon and metal organic framework material.
The feed line and the vent line each have a bypass portion for connecting the non-bypass portion to the feed end of the respective adsorbent bed and a non-bypass portion with a valve disposed thereon.
The heating line has a bypass portion for connecting the non-bypass portion to the feed end and the discharge end of the corresponding adsorbent bed, and a non-bypass portion on which a valve is provided and a heater is provided.
The gas collection line is connected to the heater through a valve.
The process applying the system specifically comprises the following steps: any one of the adsorbent beds in the system is repeatedly subjected to a cycle comprising the steps of:
(a) an adsorption step: introducing the raw material gas into the feed end of any adsorption bed through a raw material pipeline, and discharging the raw material gas serving as product gas to a gas collecting pipeline after the raw material gas passes through the adsorption bed;
(b) a heating step: feeding the gas in the heating pipeline into a heater for heating, and then introducing the gas into the discharge end of any adsorption bed to discharge the gas to an exhaust pipeline after the gas passes through the adsorption bed;
(c) pre-cooling: part of the product gas in the gas collection pipeline is introduced into the discharge end of any adsorption bed, and is discharged to a gas discharge pipeline after passing through the adsorption bed;
(d) and (3) cooling: passing a portion of the product gas in the gas collection line (which portion may be different from that in step (c)) to the discharge end of either adsorbent bed to pass through the adsorbent bed and discharge it to the heating line.
Wherein, the raw material gas in the step (a) is one of air, natural gas or mixed gas containing volatile organic compounds.
The cycle further comprises a preheating step, wherein the preheating step is positioned after the adsorption step, and a part (which can be different from the part in the steps (c) and (d)) of the product gas in the gas collecting pipeline is sent to a heater for heating and then is introduced into the discharge end of any adsorption bed, so that the product gas passes through the adsorption bed and is discharged to a gas discharge pipeline.
The cycle further comprises a pressure reduction step and a pressure increase step, wherein the pressure reduction step is positioned after the adsorption step, and the pressure reduction step reduces the pressure inside any one of the adsorption beds; the pressurization step is located after the cooling step, and the pressurization step restores the gas pressure inside any one of the adsorption beds.
The utility model discloses an above-mentioned technical scheme's beneficial effect as follows:
in the above-described aspect, the recovery of the above-described waste heat can be achieved by using a system in which a plurality of adsorption beds, for example, three adsorption beds are used, one adsorption bed is in the adsorption step while the other adsorption bed is in the heating step, and the third adsorption bed is in the cooling step, and in which, for any one of the adsorption beds in the system, the regeneration gas used in the cooling step is derived from the product gas, and the regeneration gas used in the heating step is derived from the gas discharged from the other adsorption bed in the cooling step. In addition, the system is provided with three adsorption bed streams for adsorption, and each adsorption bed is in the regeneration step twice as long as in the adsorption step, so that the flow rate of the regeneration gas can be reduced to half of that of the conventional system, thereby improving the recovery rate of the product gas. The scheme can reduce the waste heat emission of the temperature swing adsorption gas purification system and improve the product gas recovery rate, and has great energy-saving significance in industrial occasions such as air drying, natural gas treatment and the like.
Drawings
FIG. 1 is a flow diagram of a conventional temperature swing adsorption gas purification system;
fig. 2 is a system flowchart of embodiment 2 of the present invention;
fig. 3 is a system flowchart of embodiment 4 of the present invention.
Wherein: 1, a first adsorption bed; 2-adsorption bed two; 3-adsorption bed three; 4-a heating line; 5-a feed line; 6-an exhaust line; 7-gas collection line; 41-valve one; 42-valve two; 43-valve three; 44-valve four; 45-valve five; 46-valve six; 51-valve seven; 52-valve eight; 53-valve nine; 61-valve ten; 62-valve eleven; 63-valve twelve; 64-valve thirteen; 65-valve fourteen; 66-valve fifteen; 71-valve sixteen; 72-seventeen valves; 73-eighteen valves; 74-valve nineteen; 75-valve twenty; 76-valve twenty one; 401-a heater; 701-valve twenty-two.
Detailed Description
In order to make the technical problems, technical solutions and advantages to be solved by the present invention clearer, the following detailed description will be given with reference to the accompanying drawings and specific embodiments.
The utility model provides a multi-bed temperature swing adsorption gas purification system and process.
Generally parallelly connected two adsorption beds in the conventional temperature swing adsorption gas purification system in this field so that switch over the use, as shown in fig. 1, the utility model discloses the system then includes a plurality of adsorption beds and pipeline, and every adsorption bed includes feed end and discharge end, and the pipeline includes raw material pipeline, exhaust pipe line, gas collecting line and heating pipeline, and wherein the feed end of adsorption bed is connected to raw material pipeline and exhaust pipe line, and the discharge end of adsorption bed is connected to the gas collecting line, and the feed end and the discharge end of adsorption bed are connected to the heating pipeline, set up the heater on the heating pipeline.
The following description is given with reference to specific examples.
Example 1
The utility model provides a pair of gas purification process is adsorbed to multi-bed temperature swing is gone on in a plurality of adsorbent beds for example including the preferred three adsorbent bed of this embodiment. Each of the plurality of adsorbent beds is a fixed bed packed with an adsorbent (e.g., 13x molecular sieve, activated alumina). A plurality of adsorbent beds are interconnected so that during some of the steps, an adsorbent bed can exchange one or more gases with one or more other adsorbent beds. Each of the plurality of adsorption beds repeatedly performs a cycle including the following steps, but the cycles performed by the respective adsorption beds are staggered with respect to each other:
(a) an adsorption step during which a feed gas to be treated (e.g., feed natural gas) is passed into the feed end of an adsorption bed and the feed gas is discharged through the adsorption bed as a product gas to a gas collection line; as a result, most of the impurities (e.g., water vapor) in the raw gas are adsorbed and removed by the adsorbent, thereby becoming a product gas containing almost no impurities;
(b) a heating step: during this step, the gas in the heating line is sent to a heater for heating (e.g., to 180 ℃), and then passed to the discharge end of any one of the adsorption beds for discharge to the exhaust line after passing through the adsorption bed; as a result, the adsorption bed is heated, thereby desorbing a portion of the impurities in the adsorption bed;
(c) pre-cooling: part of the product gas in the gas collection pipeline is introduced into the discharge end of any adsorption bed and is discharged to a gas discharge pipeline after passing through the adsorption bed; as a result, the heat stored in the adsorbent bed is transferred toward the feed end, thereby cooling a portion of the adsorbent bed to restore a portion of its adsorption capacity;
(d) and (3) cooling: part of the product gas in the gas collection pipeline is introduced into the discharge end of any adsorption bed and is discharged to the heating pipeline after passing through the adsorption bed; as a result, the heat stored in the adsorbent bed is transferred toward the feed end until it is finally discharged out of the adsorbent bed, thereby cooling the entire adsorbent bed to restore its full adsorption capacity.
Preferably, the cycle further comprises a (a1) pressure reduction step and a (d1) pressure increase step, wherein the pressure reduction step is provided after the adsorption step and the pressure increase step is provided before the adsorption step; in practice, the operating pressure in the regeneration mode (regeneration pressure) is generally near atmospheric pressure, while the operating pressure in the adsorption mode (adsorption pressure) is generally higher than atmospheric pressure, and the pressure reduction and pressurization steps are provided to reduce fluid impact on each adsorbent bed during switching between the adsorption mode and the regeneration mode, thereby improving the operating life of the adsorbent and associated equipment, and avoiding other adverse effects due to the fluid impact phenomenon.
Preferably, the number of the adsorption beds in this embodiment is three. However, the process of the present invention is not limited to three adsorption beds, and the number of adsorption beds is at least three, and usually three or four adsorption beds are used.
The utility model discloses a technology still relates to the dislocation relation of each adsorption bed execution cycle, the interactive relation between each adsorption bed can be reflected in the dislocation relation. As a preference of this embodiment, Table 1 shows the step arrangement and cycle offset relationship of the three beds in this embodiment within one cycle. As shown in table 1, in the present embodiment, one cycle can be divided into 12 operation periods according to the step switching needs of three adsorption beds, and the adsorption beds have the following interaction relationship: the gas used by the first adsorption bed in the heating step comes from the gas discharged by the second adsorption bed in the cooling step; the gas used by the second adsorption bed in the heating step comes from the gas discharged by the third adsorption bed in the cooling step; the gas used by the adsorbent bed three in its heating step is derived from the gas discharged from the adsorbent bed one in its cooling step.
TABLE 1 arrangement of steps and cycle offset for each adsorbent bed in example 1
(a-adsorption step, a 1-depressurization step, b-heating step, c-precooling step, d-cooling step, d 1-pressurization step)
Example 2
The embodiment provides a system for implementing the process described in embodiment 1, and please refer to fig. 2, which is a flow chart of the system of the embodiment. The system mainly comprises a first adsorption bed 1, a second adsorption bed 2, a third adsorption bed 3, a heating pipeline 4, a raw material pipeline 5, an exhaust pipeline 6, a gas collecting pipeline 7 and a heater 401.
The feed ends of the first adsorption bed 1, the second adsorption bed 2 and the third adsorption bed 3 are respectively connected with the branch part of the heating pipeline 4 through a valve IV 44, a valve V45 and a valve VI 46; the feed ends of the first adsorption bed 1, the second adsorption bed 2 and the third adsorption bed 3 are respectively connected with the branch part of the raw material pipeline 5 through a seventh valve 51, an eighth valve 52 and a ninth valve 53; the feed ends of the first adsorption bed 1, the second adsorption bed 2 and the third adsorption bed 3 are respectively connected with the branch part of the exhaust pipeline 6 through a valve ten 61, a valve eleven 62 and a valve twelve 63; the discharge ends of the first adsorption bed 1, the second adsorption bed 2 and the third adsorption bed 3 are respectively connected with the branch part of the heating pipeline 4 through a first valve 41, a second valve 42 and a third valve 43; the discharge ends of the first adsorption bed 1, the second adsorption bed 2 and the third adsorption bed 3 are respectively connected with the branch part of the gas collecting pipeline 7 through a valve sixteen 71, a valve seventeenth 72 and a valve eighteen 73; a heater 401 is provided on the non-branch portion of the heating line 4.
Preferably, in the present embodiment, a thirteen valve 64 connected in parallel with the valve ten 61, a fourteen valve 65 connected in parallel with the valve eleven 62, and a fifteen valve 66 connected in parallel with the valve twelve 63 are further provided on the branch portion of the exhaust line 6, and the thirteen valve 64, the fourteen valve 65, and the fifteen valve 66 are mainly used for regulating the gas pressure.
Preferably, the branch portion of the gas collecting line 7 is further provided with a valve nineteen 74 connected in parallel with the valve sixteen 71, a valve twenty 75 connected in parallel with the valve seventeen 72, and a valve twenty-one 76 connected in parallel with the valve eighteen 73, wherein the valves nineteen 74, twenty 75 and twenty-one 76 are mainly used for regulating the gas pressure.
To further describe the specific process of the system of this embodiment for carrying out the process of example 1, the steps performed by and the operating periods experienced by each adsorbent bed will be described in detail below with reference to the operating cycle of adsorbent bed one 1 in conjunction with fig. 2:
assume the loop initialization state is: the first adsorption bed 1 is at the end of the pressurization step, the second adsorption bed 2 is in the adsorption step, the third adsorption bed 3 is in the precooling step, the heater 401 is in the closed state, and the valve state is as follows: valve eight 52, valve twelve 63, valve seventeen 72, valve nineteen 74, and valve twenty one 76 are open, with the remaining valves closed.
(a) Adsorption step
Operation period 1：
Pipeline state: the nineteen 74 valves are closed and the seven 51, sixteen 71 valves are open, and the remaining valves, the heater 401, remain unchanged in the initial state.
Adsorbent bed one 1 state: the raw material gas of the raw material line 5 enters the first adsorption bed 1 through a valve seven 51 and is then discharged to the gas collecting line 7 through a valve sixteen 71, with the result that the raw material gas becomes the product gas;
state of the adsorption bed two 2: the raw material gas of the raw material line 5 enters the second adsorption bed 2 via the valve eight 52 and is then discharged to the gas collecting line 7 via the valve seventeen 72, with the result that the raw material gas becomes a product gas;
three 3 states of the adsorption bed: a portion of the product gas from gas collection line 7 passes to adsorbent bed three 3 via valve twenty-one 76 and then to exhaust line 6 via valve twelve 63 and finally out of the system, with the result that adsorbent bed three 3 is partially cooled.
Operation period 2：
Pipeline state: the valves eight 52, seventeen 72 are closed and fourteen 65 are open, with the remaining valves, heater 401, remaining unchanged from the state of operating period 1.
Adsorbent bed one 1 state: keeping the state of the operation period 1 unchanged;
state of the adsorption bed two 2: the gas in the second adsorption bed 2 is pressure-regulated by a valve fourteen 65 and then discharged to the gas discharge line 6, and finally discharged out of the system, with the result that the pressure in the second adsorption bed 2 is reduced to the regeneration pressure;
three 3 states of the adsorption bed: the state of the operation period 1 is kept unchanged.
Operation period 3：
Pipeline state: valve twelve 63, valve fourteen 65 are closed and valve two 42, valve six 46, valve eleven 62 are open, heater 401 is open, and the remaining valves remain unchanged for operating period 2.
Adsorbent bed one 1 state: keeping the state of the operation period 2 unchanged;
state of the adsorption bed two 2: the gas in the heating pipeline 4 enters and passes through the second adsorption bed 2 through the second valve 42, then is discharged to the exhaust pipeline 6 through the eleventh valve 62, and finally is discharged out of the system, so that the second adsorption bed 2 is partially heated, and the waste heat discharged by the third adsorption bed 3 is utilized;
three 3 states of the adsorption bed: a portion of the product gas in the gas collection line 7 enters and passes through the adsorbent bed three 3 via the valve twenty-one 76 and is then discharged to the heating line 4 via the valve six 46, with the result that the adsorbent bed three 3 is completely cooled and the waste heat discharged from the adsorbent bed three 3 is recovered.
Operation period 4：
Pipeline state: valve two 42, valve six 46 are closed and valve twenty 75 is open, heater 401 is closed, and the remaining valves remain unchanged for operating period 3.
Adsorbent bed one 1 state: keeping the state of the operation period 3 unchanged;
state of the adsorption bed two 2: a portion of the product gas of gas collection line 7 enters and passes through adsorbent bed two 2 via valve twenty 75 and is then discharged to gas discharge line 6 via valve eleven 62 and ultimately out of the system, with the result that adsorbent bed two 2 is partially cooled;
three 3 states of the adsorption bed: a portion of the product gas of the gas collection line 7 enters the adsorbent bed three 3 via the valve twenty-one 76, with the result that the pressure of the adsorbent bed three 3 rises to the adsorption pressure.
Period of operation 5：
Pipeline state: valve twenty-one 76 is closed and valves nine 53 and eighteen 73 are open, the remaining valves, heater 401, remaining in the state of operating period 4.
Adsorbent bed one 1 state: keeping the state of the operation period 4 unchanged;
state of the adsorption bed two 2: keeping the state of the operation period 4 unchanged;
three 3 states of the adsorption bed: the feed gas of the feed line 5 enters and passes through the adsorption bed three 3 via the valve nine 53 and is then discharged to the gas collecting line 7 via the valve eighteen 73, with the result that the feed gas becomes a product gas.
(a1) Pressure reduction step
Period of operation 6：
Pipeline state: valve seven 51, valve sixteen 71 are closed and valve thirteen 64 are open, the remaining valves, heater 401, remain unchanged for operating period 5.
Adsorbent bed one 1 state: the gas in the adsorption bed one 1 is pressure-regulated by a valve thirteen 64 and then discharged to the exhaust line 6, and finally discharged out of the system, with the result that the pressure in the adsorption bed one 1 is reduced to the regeneration pressure;
state of the adsorption bed two 2: keeping the state of the operation period 5 unchanged;
three 3 states of the adsorption bed: the state of the operation period 5 is kept unchanged.
(b) Heating step
Operating period 7：
Pipeline state: valve eleven 62, valve thirteen 64 are closed and valve one 41, valve five 45, valve ten 61 are open, the heater 401 is open, and the remaining valves remain unchanged for operating period 6.
Adsorbent bed one 1 state: the gas in the heating pipeline 4 enters and passes through the first adsorption bed 1 through a first valve 41, then is discharged to a discharge pipeline 6 through a tenth valve 61, and finally is discharged out of the system, so that the first adsorption bed 1 is partially heated, and the waste heat discharged by the second adsorption bed 2 is utilized;
state of the adsorption bed two 2: a portion of the product gas of the gas collection line 7 enters and passes through the second adsorption bed 2 via the valve twenty 75 and is then discharged to the heating line 4 via the valve five 45, with the result that the second adsorption bed 2 is completely cooled and the waste heat discharged from the second adsorption bed 2 is recovered;
three 3 states of the adsorption bed: the state of the operation period 6 is kept unchanged.
(c) Pre-cooling step
Operating period 8：
Pipeline state: valve one 41, valve five 45 are closed and valve nineteen 74 are open, heater 401 is closed, and the remaining valves remain unchanged for operating period 7.
Adsorbent bed one 1 state: a portion of the product gas of the gas collection line 7 enters and passes through the adsorbent bed one 1 via the valve nineteen 74, is then discharged to the gas discharge line 6 via the valve ten 61, and is finally discharged out of the system, with the result that the adsorbent bed one 1 is partially cooled;
state of the adsorption bed two 2: a portion of the product gas of gas collection line 7 enters adsorbent bed two 2 via valve twenty 75, with the result that the pressure of adsorbent bed two 2 rises to the adsorption pressure;
three 3 states of the adsorption bed: the state of the operation period 7 is kept unchanged.
Operating period 9：
Pipeline state: valve twenty 75 is closed and valves eight 52, seventeen 72 are open, the remaining valves, heater 401, remain unchanged for operating period 8.
Adsorbent bed one 1 state: keeping the state of the operation period 8 unchanged;
state of the adsorption bed two 2: the raw gas of the raw gas line 5 enters and passes through the second adsorption bed 2 via the valve eight 52 and is then discharged to the gas collecting line 7 via the valve seventeen 72, with the result that the raw gas becomes a product gas;
three 3 states of the adsorption bed: the state of the operation period 8 is kept unchanged.
Operating period 10：
Pipeline state: the nine 53 and eighteen 73 valves are closed and the fifteen 66 valve is opened, and the remaining valves, the heater 401, remain unchanged for the operating period 9.
Adsorbent bed one 1 state: keeping the state of the operation period 9 unchanged;
state of the adsorption bed two 2: keeping the state of the operation period 9 unchanged;
three 3 states of the adsorption bed: the gas in the adsorption bed three 3 is pressure-regulated by the valve fifteen 66 and discharged to the gas discharge line 6, and finally discharged out of the system, with the result that the pressure in the adsorption bed three 3 is reduced to the regeneration pressure;
(d) step of Cooling
Operating period 11：
Pipeline state: valve ten 61, valve fifteen 66 are closed and valve three 43, valve four 44, valve twelve 63 are open, heater 401 is open, and the remaining valves remain unchanged for operating period 10.
Adsorbent bed one 1 state: a portion of the product gas of the gas collecting line 7 enters and passes through the adsorbent bed one 1 via the valve nineteen 74 and is then discharged to the heating line 4 via the valve four 44, with the result that the adsorbent bed one 1 is completely cooled and the waste heat discharged from the adsorbent bed one 1 is recovered;
state of the adsorption bed two 2: keeping the state of the operation period 10 unchanged;
three 3 states of the adsorption bed: the gas in the heating line 4 enters through the third valve 43 and passes through the third adsorbent bed 3, and then is discharged through the twelfth valve 63 to the exhaust line 6, and finally is discharged out of the system, with the result that the third adsorbent bed 3 is partially heated, and the waste heat discharged from the first adsorbent bed 1 is utilized.
(d1) Step of pressurizing
Operating period 12：
Pipeline state: valve three 43, valve four 44 are closed and valve twenty one 76 is open, heater 401 is closed, and the remaining valves remain unchanged for operating period 11.
Adsorbent bed one 1 state: a portion of the product gas of the gas collection line 7 enters the adsorbent bed one 1 via the valve nineteen 74, with the result that the pressure of the adsorbent bed one 1 rises to the adsorption pressure;
state of the adsorption bed two 2: keeping the state of the operation period 11 unchanged;
three 3 states of the adsorption bed: a portion of the product gas from gas collection line 7 enters and passes through adsorbent bed three 3 via valve twenty-one 76 and is subsequently discharged to gas discharge line 6 via valve twelve 63 and ultimately out of the system, with the result that adsorbent bed three 3 is partially cooled.
At this point, the loop resumes the initial state.
Example 3
The utility model provides a pair of gas purification process is adsorbed to multi-bed temperature swing carries out in a plurality of adsorption beds include the preferred three adsorption bed of this embodiment. In this embodiment, compared with embodiment 1, a preheating step (a2) is added, the preheating step is located after the adsorption step, and the preheating step feeds part of the product gas in the gas collecting line into the heater for heating and then leads the part of the product gas to the discharge end of any one of the adsorption beds, so that the part of the product gas passes through the adsorption bed and is discharged to the exhaust line.
The utility model discloses a technology still relates to the dislocation relation of each adsorption bed execution cycle, the interactive relation between each adsorption bed can be reflected in the dislocation relation. As a preference of this embodiment, Table 2 shows the step arrangement and cycle offset relationship of the three beds in this embodiment within one cycle. As shown in table 2, in the present embodiment, according to the step switching requirement of three adsorption beds, one cycle can be divided into 15 operation periods, and the following interaction relationship is provided between the adsorption beds: the gas used by the first adsorption bed in the heating step comes from the gas discharged by the second adsorption bed in the cooling step; the gas used by the second adsorption bed in the heating step comes from the gas discharged by the third adsorption bed in the cooling step; the gas used by the adsorbent bed three in its heating step is derived from the gas discharged from the adsorbent bed one in its cooling step.
TABLE 2 arrangement of steps and cycle offset for each adsorbent bed in example 3
(a-adsorption step, a 1-depressurization step, a 2-Pre-Heat step, b-heating step, c-Pre-Cooling step, d-Cooling step, d 1-pressurization step)
Example 4
The present embodiment provides a system for implementing the process described in embodiment 3, and please refer to fig. 3, which is a flow chart of the system of the present embodiment. In contrast to embodiment 2, the system of this embodiment also has a connecting line between the non-branched portion of the gas collection line 7 and the gas inlet of the heater 401, and the connecting line also has a valve twenty-two 701 for selectively feeding the product gas into the heater 401.
To further describe the specific process of the system of this embodiment for implementing the process of example 3, the steps performed by each adsorption bed and the operation period experienced by each adsorption bed will be described in detail with reference to the operation cycle of adsorption bed one 1 in conjunction with fig. 3:
assume the loop initialization state is: the first adsorption bed 1 is at the end of the pressurization step, the second adsorption bed 2 is in the adsorption step, the third adsorption bed 3 is in the precooling step, the heater 401 is in the closed state, and the valve state is as follows: valve eight 52, valve twelve 63, valve seventeen 72, valve nineteen 74, and valve twenty one 76 are open, with the remaining valves closed.
(a) Adsorption step
Operation period 1：
Pipeline state: the nineteen 74 valves are closed and the seven 51, sixteen 71 valves are open, and the remaining valves, the heater 401, remain unchanged in the initial state.
Adsorbent bed one 1 state: the raw material gas of the raw material line 5 enters the first adsorption bed 1 through a valve seven 51 and is then discharged to the gas collecting line 7 through a valve sixteen 71, with the result that the raw material gas becomes the product gas;
state of the adsorption bed two 2: the raw material gas of the raw material line 5 enters the second adsorption bed 2 via the valve eight 52 and is then discharged to the gas collecting line 7 via the valve seventeen 72, with the result that the raw material gas becomes a product gas;
three 3 states of the adsorption bed: a portion of the product gas from gas collection line 7 passes to adsorbent bed three 3 via valve twenty-one 76 and then to exhaust line 6 via valve twelve 63 and finally out of the system, with the result that adsorbent bed three 3 is partially cooled.
Operation period 2：
Pipeline state: the valves eight 52, seventeen 72 are closed and fourteen 65 are open, with the remaining valves, heater 401, remaining unchanged from the state of operating period 1.
Adsorbent bed one 1 state: keeping the state of the operation period 1 unchanged;
state of the adsorption bed two 2: the gas in the second adsorption bed 2 is pressure-regulated by a valve fourteen 65 and then discharged to the gas discharge line 6, and finally discharged out of the system, with the result that the pressure in the second adsorption bed 2 is reduced to the regeneration pressure;
three 3 states of the adsorption bed: the state of the operation period 1 is kept unchanged.
Operation period 3：
Pipeline state: valve fourteen 65 is closed and valves two 42, eleven 62, twenty-two 701 are open, heater 401 is open, and the remaining valves remain in the state of operating period 2.
Adsorbent bed one 1 state: keeping the state of the operation period 2 unchanged;
state of the adsorption bed two 2: a portion of the product gas in the gas collection line 7 is sent to the heater 401 via valve twenty-two 701 to be heated, then enters and passes through the adsorbent bed two 2 via valve two 42, and then is discharged to the gas discharge line 6 via valve eleven 62 and finally exits the system, with the result that the adsorbent bed two 2 is partially heated;
three 3 states of the adsorption bed: the state of the operation period 2 is kept unchanged.
Operation period 4：
Pipeline state: valve twelve 63, valve twenty-two 701 are closed and valve six 46 is open, the remaining valves, heater 401, remain unchanged for operating period 3.
Adsorbent bed one 1 state: keeping the state of the operation period 3 unchanged;
state of the adsorption bed two 2: the gas in the heating pipeline 4 enters and passes through the second adsorption bed 2 through the second valve 42, then is discharged to the exhaust pipeline 6 through the eleventh valve 62, and finally is discharged out of the system, so that the second adsorption bed 2 is partially heated, and the waste heat discharged by the third adsorption bed 3 is utilized;
three 3 states of the adsorption bed: a portion of the product gas in the gas collection line 7 enters and passes through the adsorbent bed three 3 via the valve twenty-one 76 and is then discharged to the heating line 4 via the valve six 46, with the result that the adsorbent bed three 3 is completely cooled and the waste heat discharged from the adsorbent bed three 3 is recovered.
Period of operation 5：
Pipeline state: valve two 42, valve six 46 are closed and valve twenty 75 is open, heater 401 is closed, and the remaining valves remain in the state of operating period 4.
Adsorbent bed one 1 state: keeping the state of the operation period 4 unchanged;
state of the adsorption bed two 2: a portion of the product gas of gas collection line 7 enters and passes through adsorbent bed two 2 via valve twenty 75 and is then discharged to gas discharge line 6 via valve eleven 62 and ultimately out of the system, with the result that adsorbent bed two 2 is partially cooled;
three 3 states of the adsorption bed: a portion of the product gas of the gas collection line 7 enters the adsorbent bed three 3 via the valve twenty-one 76, with the result that the pressure of the adsorbent bed three 3 rises to the adsorption pressure.
Period of operation 6：
Pipeline state: the twenty-one 76 valve is closed and the nine 53 and eighteen 73 valves are opened, and the remaining valves, the heater 401, remain unchanged for the operating period 5.
Adsorbent bed one 1 state: keeping the state of the operation period 5 unchanged;
state of the adsorption bed two 2: keeping the state of the operation period 5 unchanged;
three 3 states of the adsorption bed: the feed gas of the feed line 5 enters and passes through the adsorption bed three 3 via the valve nine 53 and is then discharged to the gas collecting line 7 via the valve eighteen 73, with the result that the feed gas becomes a product gas.
(a1) Pressure reduction step
Operating period 7：
Pipeline state: valve seven 51, valve sixteen 71 are closed and valve thirteen 64 are open, the remaining valves, heater 401, remain unchanged for operating period 6.
Adsorbent bed one 1 state: the gas in the adsorption bed one 1 is pressure-regulated by a valve thirteen 64 and then discharged to the exhaust line 6, and finally discharged out of the system, with the result that the pressure in the adsorption bed one 1 is reduced to the regeneration pressure;
state of the adsorption bed two 2: keeping the state of the operation period 6 unchanged;
three 3 states of the adsorption bed: the state of the operation period 6 is kept unchanged.
(a2) Preheating step
Operating period 8：
Pipeline state: valve thirteen 64 is closed while valves one 41, ten 61, twenty two 701 are open, heater 401 is open, and the remaining valves remain in the state of operating period 7.
Adsorbent bed one 1 state: a portion of the product gas in the gas collection line 7 is sent to the heater 401 via valve twenty-two 701 to be heated, then enters and passes through the adsorbent bed one 1 via valve one 41, then is discharged to the gas discharge line 6 via valve ten 61, and finally is discharged out of the system, with the result that the adsorbent bed one 1 is partially heated;
state of the adsorption bed two 2: keeping the state of the operation period 7 unchanged;
three 3 states of the adsorption bed: the state of the operation period 7 is kept unchanged.
(b) Heating step
Operating period 9：
Pipeline state: valve eleven 62, valve twenty-two 701 are closed and valve five 45 are open, the remaining valves, heater 401, remain unchanged for operating period 8.
Adsorbent bed one 1 state: the gas in the heating pipeline 4 enters and passes through the first adsorption bed 1 through a first valve 41, then is discharged to a discharge pipeline 6 through a tenth valve 61, and finally is discharged out of the system, so that the first adsorption bed 1 is partially heated, and the waste heat discharged by the second adsorption bed 2 is utilized;
state of the adsorption bed two 2: a portion of the product gas of the gas collection line 7 enters and passes through the second adsorption bed 2 via the valve twenty 75 and is then discharged to the heating line 4 via the valve five 45, with the result that the second adsorption bed 2 is completely cooled and the waste heat discharged from the second adsorption bed 2 is recovered;
three 3 states of the adsorption bed: the state of the operation period 8 is kept unchanged.
(c) Pre-cooling step
Operating period 10：
Pipeline state: valve one 41, valve five 45 are closed and valve nineteen 74 are open, heater 401 is closed, and the remaining valves remain in the state of operational period 9.
Adsorbent bed one 1 state: a portion of the product gas of the gas collection line 7 enters and passes through the adsorbent bed one 1 via the valve nineteen 74, is then discharged to the gas discharge line 6 via the valve ten 61, and is finally discharged out of the system, with the result that the adsorbent bed one 1 is partially cooled;
state of the adsorption bed two 2: a portion of the product gas of gas collection line 7 enters adsorbent bed two 2 via valve twenty 75, with the result that the pressure of adsorbent bed two 2 rises to the adsorption pressure;
three 3 states of the adsorption bed: the state of the operation period 9 is kept unchanged.
Operating period 11：
Pipeline state: valve twenty 75 is closed and valves eight 52, seventeen 72 are open, the remaining valves, heater 401, remain unchanged for operating period 10.
Adsorbent bed one 1 state: keeping the state of the operation period 10 unchanged;
state of the adsorption bed two 2: the raw gas of the raw gas line 5 enters and passes through the second adsorption bed 2 via the valve eight 52 and is then discharged to the gas collecting line 7 via the valve seventeen 72, with the result that the raw gas becomes a product gas;
three 3 states of the adsorption bed: the state of the operation period 10 is kept unchanged.
Operating period 12：
Pipeline state: the nine 53 and eighteen 73 valves are closed and the fifteen 66 valve is opened, and the remaining valves, the heater 401, remain unchanged for the operating period 11.
Adsorbent bed one 1 state: keeping the state of the operation period 11 unchanged;
state of the adsorption bed two 2: keeping the state of the operation period 11 unchanged;
three 3 states of the adsorption bed: the gas in the adsorption bed three 3 is pressure-regulated by the valve fifteen 66 and discharged to the gas discharge line 6, and finally discharged out of the system, with the result that the pressure in the adsorption bed three 3 is reduced to the regeneration pressure;
operating period 13：
Pipeline state: valve fifteen 66 is closed while valves three 43, twelve 63, twenty-two 701 are open, heater 401 is open, and the remaining valves remain in the state of operating period 12.
Adsorbent bed one 1 state: keeping the state of the operation period 12 unchanged;
state of the adsorption bed two 2: keeping the state of the operation period 12 unchanged;
three 3 states of the adsorption bed: a portion of the product gas in the gas collection line 7 is sent through the heater 401 via valve twenty-two 701 to be heated, then through valve three 43 into and through adsorbent bed three 3, then through valve twelve 63 to the gas discharge line 6 and finally out of the system, with the result that adsorbent bed three 3 is partially heated.
(d) Step of Cooling
Operating period 14：
Pipeline state: valve ten 61, valve twenty-two 701 are closed and valve four 44 are open, the remaining valves, heater 401, remain unchanged for operating period 13.
Adsorbent bed one 1 state: a portion of the product gas of the gas collecting line 7 enters and passes through the adsorbent bed one 1 via the valve nineteen 74 and is then discharged to the heating line 4 via the valve four 44, with the result that the adsorbent bed one 1 is completely cooled and the waste heat discharged from the adsorbent bed one 1 is recovered;
state of the adsorption bed two 2: keeping the state of the operation period 13 unchanged;
three 3 states of the adsorption bed: the gas in the heating line 4 enters through the third valve 43 and passes through the third adsorbent bed 3, and then is discharged through the twelfth valve 63 to the exhaust line 6, and finally is discharged out of the system, with the result that the third adsorbent bed 3 is partially heated, and the waste heat discharged from the first adsorbent bed 1 is utilized.
(d1) Step of pressurizing
Operating period 15：
Pipeline state: valve three 43, valve four 44 are closed and valve twenty one 76 is open, heater 401 is closed, and the remaining valves remain unchanged for operating period 14.
Adsorbent bed one 1 state: a portion of the product gas of the gas collection line 7 enters the adsorbent bed one 1 via the valve nineteen 74, with the result that the pressure of the adsorbent bed one 1 rises to the adsorption pressure;
state of the adsorption bed two 2: keeping the state of the operation period 14 unchanged;
three 3 states of the adsorption bed: a portion of the product gas from gas collection line 7 enters and passes through adsorbent bed three 3 via valve twenty-one 76 and is subsequently discharged to gas discharge line 6 via valve twelve 63 and ultimately out of the system, with the result that adsorbent bed three 3 is partially cooled.
At this point, the loop resumes the initial state.
The foregoing is a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of improvements and decorations can be made without departing from the principle of the present invention, and these improvements and decorations should also be regarded as the protection scope of the present invention.
Claims (6)
1. A multi-bed temperature swing adsorption gas purification system is characterized in that: the adsorption bed comprises a plurality of adsorption beds and pipelines, wherein each adsorption bed comprises a feeding end and a discharging end, each pipeline comprises a raw material pipeline, an exhaust pipeline, a gas collecting pipeline and a heating pipeline, the raw material pipeline and the exhaust pipeline are connected with the feeding ends of the adsorption beds, the gas collecting pipeline is connected with the discharging ends of the adsorption beds, the heating pipelines are connected with the feeding ends and the discharging ends of the adsorption beds, and heaters are arranged on the heating pipelines.
2. The multi-bed temperature swing adsorption gas purification system of claim 1, wherein: the adsorption bed is one of a horizontal axial flow adsorption bed, a vertical axial flow adsorption bed or a vertical radial flow adsorption bed, the number of the adsorption beds is not less than three, and at least one layer of adsorbent is filled in the adsorption bed.
3. The multi-bed temperature swing adsorption gas purification system of claim 2, wherein: the adsorbent is one of molecular sieve, alumina, silica gel, active carbon and metal organic framework material.
4. The multi-bed temperature swing adsorption gas purification system of claim 1, wherein: the feed line and the vent line each have a bypass portion for connecting the non-bypass portion to the feed end of the respective adsorbent bed and a non-bypass portion with a valve disposed thereon.
5. The multi-bed temperature swing adsorption gas purification system of claim 1, wherein: the heating line has a bypass portion for connecting the non-bypass portion to the feed end and the discharge end of the corresponding adsorbent bed, and a non-bypass portion on which a heater is provided.
6. The multi-bed temperature swing adsorption gas purification system of claim 1, wherein: the gas collection line is connected to the heater through a valve.
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| CN109966860A (en) * | 2019-04-16 | 2019-07-05 | 北京科技大学 | More temperature swing adsorption gas purification systems of one kind and technique |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109966860A (en) * | 2019-04-16 | 2019-07-05 | 北京科技大学 | More temperature swing adsorption gas purification systems of one kind and technique |
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