CN221412658U - Treatment system for improving adsorption capacity of molecular sieve - Google Patents
Treatment system for improving adsorption capacity of molecular sieve Download PDFInfo
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- CN221412658U CN221412658U CN202323084955.3U CN202323084955U CN221412658U CN 221412658 U CN221412658 U CN 221412658U CN 202323084955 U CN202323084955 U CN 202323084955U CN 221412658 U CN221412658 U CN 221412658U
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- 238000001179 sorption measurement Methods 0.000 title claims abstract description 173
- 239000002808 molecular sieve Substances 0.000 title claims abstract description 29
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 title claims abstract description 29
- 230000008929 regeneration Effects 0.000 claims abstract description 157
- 238000011069 regeneration method Methods 0.000 claims abstract description 157
- 238000007664 blowing Methods 0.000 claims abstract description 71
- 238000000746 purification Methods 0.000 claims abstract description 30
- 230000001105 regulatory effect Effects 0.000 claims abstract description 27
- 230000001276 controlling effect Effects 0.000 claims abstract description 9
- 239000007788 liquid Substances 0.000 claims description 11
- 239000002994 raw material Substances 0.000 claims description 9
- 230000005465 channeling Effects 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 4
- 238000012545 processing Methods 0.000 claims description 4
- 238000004200 deflagration Methods 0.000 claims description 3
- 230000002708 enhancing effect Effects 0.000 claims 6
- 230000000274 adsorptive effect Effects 0.000 claims 5
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- 238000001035 drying Methods 0.000 abstract description 8
- 238000000926 separation method Methods 0.000 abstract description 8
- 230000009471 action Effects 0.000 abstract description 2
- 239000003245 coal Substances 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract description 2
- 230000002035 prolonged effect Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 98
- 230000001172 regenerating effect Effects 0.000 description 12
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 8
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- FFBHFFJDDLITSX-UHFFFAOYSA-N benzyl N-[2-hydroxy-4-(3-oxomorpholin-4-yl)phenyl]carbamate Chemical compound OC1=C(NC(=O)OCC2=CC=CC=C2)C=CC(=C1)N1CCOCC1=O FFBHFFJDDLITSX-UHFFFAOYSA-N 0.000 description 6
- 239000004215 Carbon black (E152) Substances 0.000 description 4
- 239000003463 adsorbent Substances 0.000 description 4
- 229910021529 ammonia Inorganic materials 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 239000003949 liquefied natural gas Substances 0.000 description 4
- 229920006395 saturated elastomer Polymers 0.000 description 4
- 229910001868 water Inorganic materials 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 2
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- 238000012986 modification Methods 0.000 description 2
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- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
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- 238000013461 design Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
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- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
The utility model belongs to the technical field of coke oven coal chemical industry, and discloses a treatment system for improving adsorption capacity of a molecular sieve. The regeneration cold outlet program control valves are respectively arranged on the regeneration cold outlets of the three adsorption towers in the existing cryogenic separation drying purification unit, the regeneration hot blowing inlets of the three adsorption towers are respectively provided with the regeneration hot inlet program control valves, and meanwhile, a regeneration gas regulating and controlling pipeline is connected between a regeneration gas supply pipeline and a regeneration cold blowing circulating pipeline, and the regeneration gas regulating and controlling pipeline is provided with the regulating program control valves. According to the utility model, the central control DCS system orderly controls each program control valve of the three adsorption towers under the action of the adjusting program control valves, and the adsorption and regeneration processes of the three adsorption purification towers are the same, and the whole adsorption and regeneration processes are automatically switched and circulated by the program control valves according to a set time sequence, so that the hot blowing regeneration time of the molecular sieve is prolonged, and when the molecular sieve is in the later stage of service life, the regeneration time can be effectively improved, and the regeneration efficiency is further improved.
Description
Technical Field
The utility model belongs to the technical field of coke oven coal chemical industry, and particularly relates to a treatment system for improving adsorption capacity of a molecular sieve.
Background
The traditional process flow of the device for preparing liquefied natural gas from coke oven gas is that the coke oven gas enters a cryogenic separation drying purification unit after impurity removal, deoxidation and desulfurization and decarburization, and the drying purification unit adopts molecular sieve adsorption to remove trace H2O, CO2, benzene, ammonia, heavy hydrocarbon and other components in the coke oven gas, so that the H2O in the coke oven gas is less than or equal to 1ppm, CO2 is less than or equal to 1ppm, ammonia is less than or equal to 0.1ppm, heavy hydrocarbon is less than or equal to 1ppm, and the coke oven gas after deep purification enters a cold box for cryogenic separation to produce LNG. In the process for preparing liquefied natural gas from coke oven gas, the cryogenic separation drying purification unit mainly adopts three adsorption purification towers for adsorption regeneration, and the three adsorption purification towers regenerate the molecular sieve by adopting a method of combining Pressure Swing (PSA) and Temperature Swing (TSA) through a composite bed layer of active alumina, a 4A molecular sieve and a 13X molecular sieve, wherein the operating pressure is 3.5 MPa; and (3) carrying out hot blowing regeneration by using 3.8MPa.G saturated steam, and hot blowing to 220 ℃. And after the adsorption purification tower in the adsorption state is saturated, switching to a second cold-blown adsorption purification tower for later use, and then reducing the pressure, hot-blowing regeneration, cold blowing and pressurizing for later use after the saturated adsorption purification tower is saturated. The complete cycle period of each adsorption purification tower is 24h, the adsorption state is set to 8h, the hot blowing state is set to 7.5h, the cold blowing state is set to 7.5h, the standby state is switched to 0.5h, and the adsorption, hot blowing and cold blowing time can be timely adjusted according to the molecular sieve operation time, the purified gas component condition and the actual operation working condition, and the three adsorption purification towers are switched for recycling. However, when water, CO 2, ammonia and heavy hydrocarbon in the coke oven gas at the outlet of the drying and purifying unit exceed the standard, the fin heat exchanger in the cold box is frozen and blocked, so that the running period of the cold box is shortened.
At present, the cryogenic separation drying purification unit has the following three problems: 1. when the program enters the pressurizing process, the tower A must end the hot blowing process and enter the waiting process ①, the program time of the waiting process ① is consistent with that of the pressurizing process, and the waiting process is wasteful in regeneration time and reduces the regeneration efficiency. 2. When the molecular sieve in the adsorption purification tower is at the end of the service life, a longer hot blowing process is needed to improve the regeneration efficiency, and the current technological process cannot meet the requirements. 3. The raw material gas is used for pressurizing in the pressurizing process, and in the pressurizing process, the regenerated gas is in a torch emptying state and is not fully utilized, so that waste is caused.
Therefore, when the molecular sieve in the present stage is operated to the later stage, whether the regeneration time is enough or not and whether the regeneration is thorough or not greatly influences the adsorption capacity of the regenerated molecular sieve, which not only influences the operation period of the cold box, but also further influences the production process of liquefied natural gas from coke oven gas. Therefore, how to improve the regeneration efficiency of molecular sieves has become an important issue to be solved in the industry.
Disclosure of utility model
Aiming at the problems existing in the molecular sieve operation at the present stage in the background technology, the utility model provides a treatment system for improving the adsorption capacity of a molecular sieve.
In order to achieve the above purpose, the utility model adopts the following technical scheme: the treatment system for improving the adsorption capacity of the molecular sieve comprises a regenerated gas heater, an adsorption tower A, an adsorption tower B and an adsorption tower C, wherein the inlet of the regenerated gas heater is connected with a raw gas main pipeline, the outlet of the regenerated gas heater is connected with three raw gas inlets of the adsorption tower A, the adsorption tower B and the adsorption tower C through raw gas supply pipelines, a first adsorption inlet program control valve, a second adsorption inlet program control valve and a third adsorption inlet program control valve are respectively arranged on the three raw gas branch pipelines, three purified gas outlets of the adsorption tower A, the adsorption tower B and the adsorption tower C are connected with a purified gas discharge pipeline through three purified gas branch pipelines, a first adsorption outlet program control valve, a second adsorption outlet program control valve and a third adsorption outlet program control valve are respectively arranged on the three purified gas branch pipelines, the three regeneration gas inlets of the adsorption tower A, the adsorption tower B and the adsorption tower C are connected with a regeneration gas supply pipeline through three paths of regeneration gas branch pipes, a first regeneration cold blowing port program-controlled valve, a second regeneration cold blowing port program-controlled valve and a third regeneration cold blowing port program-controlled valve are respectively arranged on the three paths of regeneration gas branch pipes, the regeneration cold outlet and the regeneration hot blowing port of the adsorption tower A, the regeneration cold outlet and the regeneration hot blowing port of the adsorption tower B and the regeneration cold outlet and the regeneration hot blowing port of the adsorption tower C are respectively connected through regeneration cold blowing circulation pipelines, a gas-liquid separator is arranged on the regeneration cold blowing circulation pipeline, a steam supply pipeline and a steam loop pipeline are respectively connected to a heating medium inlet and a heating medium outlet of the gas-liquid separator for providing a required steam heat source for the gas-liquid separator, and the adsorption tower A, the three regeneration cold outlets of the adsorption tower B and the adsorption tower C are respectively provided with a first regeneration cold outlet program control valve, a second regeneration cold outlet program control valve and a third regeneration cold outlet program control valve, the three regeneration hot blowing inlets of the adsorption tower A, the adsorption tower B and the adsorption tower C are respectively provided with a first regeneration hot inlet program control valve, a second regeneration hot inlet program control valve and a third regeneration hot inlet program control valve, a regeneration gas regulating pipeline is connected between a regeneration gas supply pipeline and a regeneration cold blowing circulation pipeline, one end of the regeneration gas regulating pipeline is connected to the regeneration gas supply pipeline, the other end of the regeneration gas regulating pipeline is connected to the gas phase inlet end of the gas-liquid separator, the regeneration gas regulating pipeline is provided with a regulating program control valve, and the signal input ends of all the program control valves are connected with a central control DCS system.
As a further supplementary explanation of the above technical scheme, the three regeneration heat outlets of the adsorption tower a, the adsorption tower B and the adsorption tower C are connected with an evacuation line through three paths of regeneration heat branch pipes, the three paths of regeneration heat branch pipes are respectively provided with a first regeneration heat outlet program control valve, a second regeneration heat outlet program control valve and a third regeneration heat outlet program control valve, the outside of the evacuation line is connected with a fire cabinet for burning evacuated regenerated gas, and the signal input ends of the three regeneration heat outlet program control valves are respectively connected with a central control DCS system.
As a further supplementary explanation of the above technical solution, the three pressure relief outlets of the adsorption tower a, the adsorption tower B and the adsorption tower C are respectively connected with the emptying pipeline through three pressure relief branch pipes, the three pressure relief branch pipes are respectively provided with a first pressure relief program control valve, a second pressure relief program control valve and a third pressure relief program control valve, the three pressure charging inlets of the adsorption tower a, the adsorption tower B and the adsorption tower C are respectively connected with the purified gas discharge pipeline through three pressure charging branch pipes, and the three pressure charging branch pipes are respectively provided with a first pressure charging program control valve, a second pressure charging program control valve and a third pressure charging program control valve.
As a further supplementary illustration of the above technical solution, a flame arrester is mounted on the evacuation line, which prevents sparks in the fire cabinet from channeling into the evacuation line for deflagration.
As a further supplementary illustration of the above technical solution, a regeneration gas discharge line is connected between the evacuation line and the regeneration gas supply line, on which a discharge program-controlled valve is installed, the signal input of which is connected with the central control DCS system.
As a further supplementary illustration of the above technical solution, a second non-return valve is mounted on the regeneration gas discharge line, the second non-return valve being used to prevent the regeneration gas from channeling between the evacuation line and the regeneration gas supply line, thereby ensuring safe operation of the treatment system.
As a further supplementary explanation of the above technical scheme, the regenerated gas regulating pipeline is provided with a first check valve, and the first check valve is used for preventing regenerated gas between the regenerated cold blowing circulating pipeline and the regenerated gas regulating pipeline from channeling, so that safe operation of the treatment system is ensured.
Compared with the prior art, the utility model has the following advantages:
1. The utility model uses the same adsorption and regeneration processes of the three adsorption purification towers, the whole adsorption and regeneration process is automatically switched and circulated by the program control valve according to the set time sequence, and an operator can adjust the program time according to the actual needs to control the adsorption and regeneration process. Therefore, the scheme provided by the utility model prolongs the hot blowing regeneration time of the molecular sieve, and can effectively improve the regeneration time and further improve the regeneration efficiency when the molecular sieve is in the later life.
2. According to the utility model, the regenerated gas regulating and controlling pipeline is connected with the regenerated gas supply pipeline and the regenerated cold blowing circulating pipeline, and the regulating program control valve is arranged on the regenerated gas regulating and controlling pipeline, so that each program control valve of the three adsorption towers is orderly controlled by the central control DCS system under the action of the regulating program control valve, and the adsorption and regeneration flow of the molecular sieve three towers is improved.
3. According to the utility model, the exhaust pipeline is connected with the regenerated gas supply pipeline through the regenerated gas exhaust pipeline, and the exhaust program control valve is arranged on the regenerated gas exhaust pipeline, so that the regenerated gas can be effectively prevented from being exhausted through the improvement measures, and the resource utilization rate is further improved.
Drawings
FIG. 1 is a block diagram of a processing system of a cryogenic separation dry purification unit of the present utility model.
In the figure: the regenerated gas heater is 1, the adsorption tower A is 2, the adsorption tower B is 3, the adsorption tower C is 4, the gas-liquid separator is 5, the discharge program control valve is 6, the regulation program control valve is 7, the first check valve is 8, the second check valve is 9, and the flame arrester is 10.
The raw material gas main pipeline is 100 and is connected, the raw material gas supply pipeline is 200, the purified gas discharge pipeline is 300, the emptying pipeline is 400, the regenerated gas supply pipeline is 500, the regenerated cold blowing circulation pipeline is 600, the regenerated gas regulating and controlling pipeline is 700, the regenerated gas discharge pipeline is 800, the steam supply pipeline is 901 and the steam loop pipeline is 902.
In the present processing system, each of the programmable valves includes: the first adsorption inlet programming valve is 201, the first pressure relief programming valve is 202, the first regeneration heat outlet programming valve is 203, the first regeneration cold outlet programming valve is 204, the first adsorption outlet programming valve is 205, the first pressurization programming valve is 206, the first regeneration cold blowing port programming valve is 207, and the first regeneration heat inlet programming valve is 208; the second adsorption inlet program control valve is 301, the second pressure relief program control valve is 302, the second regeneration hot outlet program control valve is 303, the second regeneration cold outlet program control valve is 304, the second adsorption outlet program control valve is 305, the second pressurizing program control valve is 306, the second regeneration cold blowing inlet program control valve is 307, and the second regeneration hot inlet program control valve is 308; the third adsorption inlet program control valve is 401, the third pressure relief program control valve is 402, the third regeneration hot outlet program control valve is 403, the third regeneration cold outlet program control valve is 404, the third adsorption outlet program control valve is 405, the third pressurizing program control valve is 406, the third regeneration cold blowing inlet program control valve is 407, and the third regeneration hot inlet program control valve is 408.
Detailed Description
In order to further illustrate the technical solution of the present utility model, we will further describe the present utility model by two examples according to the on-site modification implementation with reference to fig. 1.
As shown in fig. 1, in the existing cryogenic separation, drying and purifying unit, the existing cryogenic separation, drying and purifying unit mainly comprises a regeneration gas heater 1, an adsorption tower A2, an adsorption tower B3 and an adsorption tower C4, wherein an inlet of the regeneration gas heater 1 is connected with a raw gas main pipeline 100, an outlet of the regeneration gas heater 1 is connected with three raw gas inlets of the adsorption tower A2, the adsorption tower B3 and the adsorption tower C4 through a raw gas supply pipeline 200, a first adsorption inlet program control valve 201, a second adsorption inlet program control valve 301 and a third adsorption inlet program control valve 401 are respectively installed on the three raw gas branch pipelines, three purified gas outlets of the adsorption tower A2, the adsorption tower B3 and the adsorption tower C4 are connected with a purified gas discharge pipeline 300 through three purified gas branch pipelines, a first adsorption outlet program control valve 205, a second adsorption outlet program control valve 305 and a third adsorption outlet program control valve 405 are respectively installed on the three purified gas branch pipelines, and three regeneration gas outlets of the adsorption tower A2, the adsorption tower B3 and the adsorption tower C4 are connected with the regeneration gas supply pipeline 500 through three purified gas branch pipelines.
Example 1
As shown in fig. 1, a treatment system for improving adsorption capacity of a molecular sieve is provided, a first regenerative cold blowing port program control valve 207, a second regenerative cold blowing port program control valve 307 and a third regenerative cold blowing port program control valve 407 are respectively installed on the three paths of regenerated gas branch pipes, the regenerative cold outlet and the regenerative hot blowing port of the adsorption tower A2, the regenerative cold outlet and the regenerative hot blowing port of the adsorption tower B3 and the regenerative cold outlet and the regenerative hot blowing port of the adsorption tower C4 are respectively connected through a regenerative cold blowing circulation pipeline 600, a gas-liquid separator 5 is installed on the regenerative cold blowing circulation pipeline 600, a steam supply pipeline 901 and a steam loop pipeline 902 are respectively connected to a heat medium inlet and a heat medium outlet of the gas-liquid separator 5 to provide a required steam heat source for the same, a first regeneration cold outlet program control valve 204, a second regeneration cold outlet program control valve 304 and a third regeneration cold outlet program control valve 404 are respectively arranged on the three regeneration cold outlets of the adsorption tower A2, the adsorption tower B3 and the adsorption tower C4, a first regeneration hot inlet program control valve 208, a second regeneration hot inlet program control valve 308 and a third regeneration hot inlet program control valve 408 are respectively arranged on the three regeneration hot blowing inlets of the adsorption tower A2, the adsorption tower B3 and the adsorption tower C4, a regeneration gas regulating pipeline 700 is connected between the regeneration gas supply pipeline 500 and the regeneration cold blowing circulation pipeline 600, one end of the regeneration gas regulating pipeline 700 is connected to the regeneration gas supply pipeline 500, the other end is connected to the gas inlet end of the gas-liquid separator 5, a regulating check valve 7 and a first back-flow valve 8 are respectively arranged on the regeneration gas regulating pipeline 700, the first back-flow valve 8 is used for preventing gas interaction between the regeneration cold blowing circulation pipeline 600 and the regeneration gas regulating pipeline 700, thereby ensuring the safe operation of the processing system. The three regeneration heat outlets of the adsorption tower A2, the adsorption tower B3 and the adsorption tower C4 are connected with an evacuation pipeline 400 through three paths of regeneration heat branch pipes, a first regeneration heat outlet program control valve 203, a second regeneration heat outlet program control valve 303 and a third regeneration heat outlet program control valve 403 are respectively arranged on the three paths of regeneration heat branch pipes, and a fire cabinet is connected outside the evacuation pipeline 400 for combusting evacuated regenerated gas. The three pressure relief outlets of the adsorption tower A2, the adsorption tower B3 and the adsorption tower C4 are respectively connected with the evacuation pipeline 400 through three pressure relief branch pipes, a first pressure relief program control valve 202, a second pressure relief program control valve 302 and a third pressure relief program control valve 402 are respectively arranged on the three pressure relief branch pipes, the three pressure charging inlets of the adsorption tower A2, the adsorption tower B3 and the adsorption tower C4 are respectively connected with the purified gas discharge pipeline 300 through three pressure charging branch pipes, and a first pressure charging program control valve 206, a second pressure charging program control valve 306 and a third pressure charging program control valve 406 are respectively arranged on the three pressure charging branch pipes. In this embodiment, the signal input ends of all the program control valves are connected with the central control DCS system.
As a preferred implementation of the above example, a flame arrestor 10 is mounted on the evacuation line 400, the flame arrestor 10 preventing sparks in a fire cabinet from channeling into the evacuation line 400 for deflagration.
Example two
As shown in fig. 1, in order to avoid the emptying of the regenerated gas and improve the resource utilization rate, the following scheme is supplemented in the first embodiment: a regenerated gas discharge pipeline 800 is connected between the evacuation pipeline 400 and the regenerated gas supply pipeline 500, a discharge program control valve 6 and a second check valve 9 are respectively installed on the regenerated gas discharge pipeline 800, and the second check valve 9 is used for preventing regenerated gas between the evacuation pipeline 400 and the regenerated gas supply pipeline 500 from channeling each other, so that safe operation of a treatment system is ensured. The signal input end of the emission program control valve 6 is connected with the central control DCS system.
Referring to table 1, we take adsorption purification column a as an example: the raw material gas enters an adsorption purification tower A in an adsorption state from top to bottom through a program control valve, water, carbon dioxide, ammonia, heavy hydrocarbon and the like in the raw material gas are adsorbed under the selective adsorption of an adsorbent, and the gas which is not adsorbed enters a cold box liquefying process after mercury removal and dust filtration. When the front edge (called adsorption front edge) of the mass transfer area of the adsorbed impurities reaches the reserved section of the bed layer outlet and the adsorption time is satisfied, the procedure is transferred to the next step, the adsorption inlet program control valve and the adsorption outlet program control valve of the adsorption tower are closed, the adsorption is stopped, and the adsorption bed starts to transfer to the regeneration process:
Step 1: pressure relief process (25 min): after the adsorption process is finished, opening a pressure relief regulating valve, releasing pressure to 0.3MPa.G for the adsorption purification tower, and after the pressure relief time is met, transferring the program to the next step;
Step 2: hot blowing process ① (300 min): after the pressure relief process is finished, opening a regenerated heat blowing inlet program control valve and an outlet program control valve, enabling regenerated gas to enter an adsorption purification tower, reversely purging an adsorbent bed layer, and when the outlet temperature of the adsorption purification tower is up to about 190 ℃, proving that adsorbed impurities are completely desorbed, regenerating the adsorbent of the adsorption purification tower, and when the heat blowing time is met, transferring the procedure to the next step;
Step 3: hot blowing process ② (80 min): when the hot blowing process ① is finished, the regenerated hot blowing inlet program control valve and the outlet program control valve of the tower A are kept in an open state, the regenerated gas discharging program control valve is kept in a closed state, the regenerated gas is opened to the regenerated hot blower inlet program control valve, the regenerated gas enters the cold medium end inlet of the regenerated gas hot blower through a newly added pipeline, and enters the tower A after hot blowing, the hot blowing process of the tower A is continued, and when the hot blowing process ② time is met, the process is shifted to the next step;
Step 4: wait process ① (25 min): when the waiting process ① ends, the process goes to the waiting process ②, and the tower B and the tower C are in the co-adsorption stage;
Step 5: wait process ② (25 min): when the waiting process ② is finished, the process is transferred to a waiting process ③, the tower B is in a pressure release process, and the tower C is in an adsorption process;
Step 6: cold blowing process (300 min): when the waiting process ② is finished, opening a regenerated cold blowing inlet program control valve and an regenerated cold blowing outlet program control valve, enabling regenerated gas to enter an adsorption purification tower in the cold blowing process, reversely purging an adsorbent bed layer to enable the temperature of the bed layer to be reduced to be less than 40 ℃, and when the cold blowing time is met, finishing the cold blowing process, and transferring the procedure to the next step;
Step 7: pressurizing process (80 min): and after the cold blowing process is finished, opening a pressurizing regulating valve to pressurize the adsorption purification tower, stopping pressurizing after the pressurizing time is met and transferring the process to the next step (adsorption process), wherein the pressure of the adsorption purification tower reaches 3.5MPa.G of the raw material gas main pipe.
Table 1 shows the program-controlled time schedule after modification
While the principal features and advantages of the present utility model have been shown and described, it will be apparent to those skilled in the art that the detailed description of the utility model is not limited to the details of the foregoing exemplary embodiments, but is capable of other embodiments without departing from the spirit or essential characteristics of the utility model, and the inventive concept and design concept of the utility model shall be equally included in the scope of the utility model disclosed in the appended claims. The present embodiments are, therefore, to be considered in all respects as illustrative and not restrictive, the scope of the utility model being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein.
Furthermore, it should be understood that although the present disclosure describes embodiments, not every embodiment is provided with a separate embodiment, and that this description is provided for clarity only, and that the disclosure is not limited to the embodiments described in detail below, and that the embodiments described in the examples may be combined as appropriate to form other embodiments that will be apparent to those skilled in the art.
Claims (7)
1. The utility model provides a promote processing system of molecular sieve adsorption capacity, including regeneration gas heater (1), adsorption tower A (2), adsorption tower B (3) and adsorption tower C (4), the import of regeneration gas heater (1) is connected with raw material gas parent line (100), the export of regeneration gas heater (1) divide three feed gas import that three routes raw material gas branch pipe are connected with adsorption tower A (2), adsorption tower B (3) and adsorption tower C (4) install first adsorption inlet program control valve (201), second adsorption inlet program control valve (301), third adsorption inlet program control valve (401) respectively on three routes raw material gas branch pipe, three purification gas export of adsorption tower A (2), adsorption tower B (3) and adsorption tower C (4) are connected with purification gas discharge pipeline (300) through three routes purification gas branch pipe install first adsorption outlet program control valve (205), second adsorption outlet valve (305), third adsorption outlet program control valve (405) respectively on the three routes purification gas branch pipe, its characterized in that program control valve: three regeneration gas inlets of the adsorption tower A (2), the adsorption tower B (3) and the adsorption tower C (4) are respectively connected with a regeneration gas supply pipeline (500) through three paths of regeneration gas branch pipes, a first regeneration cold blowing port program control valve (207), a second regeneration cold blowing port program control valve (307) and a third regeneration cold blowing port program control valve (407) are respectively arranged on the three paths of regeneration gas branch pipes, a regeneration cold outlet and a regeneration hot blowing port of the adsorption tower A (2), a regeneration cold outlet and a regeneration hot blowing port of the adsorption tower B (3) and a regeneration cold outlet and a regeneration hot blowing port of the adsorption tower C (4) are respectively connected through a regeneration cold blowing circulation pipeline (600), a gas-liquid separator (5) is arranged on the regeneration cold blowing circulation pipeline (600), a steam supply pipeline (901), a steam circuit (902) is respectively connected with a heating medium inlet and a heating medium outlet of the gas-liquid separator (5) to supply a required steam heat source, the regeneration cold outlet of the adsorption tower A (2), the adsorption tower B (3) and the three regeneration cold outlet and the regeneration hot blowing port of the adsorption tower C (4) are respectively provided with the first regeneration cold blowing port program control valve (204), and the regeneration cold outlet (204) are respectively arranged on the regeneration cold outlet of the regeneration cold blowing valve (2) The three regeneration hot blowing inlets of the adsorption tower B (3) and the adsorption tower C (4) are respectively provided with a first regeneration hot inlet program control valve (208), a second regeneration hot inlet program control valve (308) and a third regeneration hot inlet program control valve (408), a regeneration gas regulating and controlling pipeline (700) is connected between a regeneration gas supply pipeline (500) and a regeneration cold blowing circulation pipeline (600), one end of the regeneration gas regulating and controlling pipeline (700) is connected to the regeneration gas supply pipeline (500), the other end of the regeneration gas regulating and controlling pipeline is connected to the gas phase inlet end of the gas-liquid separator (5), a regulating program control valve (7) is arranged on the regeneration gas regulating and controlling pipeline (700), and the signal input ends of all the program control valves are connected with a central control DCS system.
2. A treatment system for enhancing the adsorptive capacity of a molecular sieve as claimed in claim 1, wherein: the three regeneration heat outlets of the adsorption tower A (2), the adsorption tower B (3) and the adsorption tower C (4) are connected with an emptying pipeline (400) through three paths of regeneration heat branch pipes, a first regeneration heat outlet program control valve (203), a second regeneration heat outlet program control valve (303) and a third regeneration heat outlet program control valve (403) are respectively arranged on the three paths of regeneration heat branch pipes, the emptying pipeline (400) is externally connected with a fire cabinet for burning and emptying regenerated gas, and signal input ends of the three regeneration heat outlet program control valves are respectively connected with a central control DCS system.
3. A treatment system for enhancing the adsorptive capacity of a molecular sieve as claimed in claim 2, wherein: the three pressure relief outlets of the adsorption tower A (2), the adsorption tower B (3) and the adsorption tower C (4) are respectively connected with the emptying pipeline (400) through three pressure relief branch pipes, a first pressure relief program control valve (202), a second pressure relief program control valve (302) and a third pressure relief program control valve (402) are respectively arranged on the three pressure relief branch pipes, three charging inlets of the adsorption tower A (2), the adsorption tower B (3) and the adsorption tower C (4) are respectively connected with the purified gas discharge pipeline (300) through three pressure relief branch pipes, and a first charging program control valve (206), a second charging program control valve (306) and a third charging program control valve (406) are respectively arranged on the three pressure relief branch pipes.
4. A treatment system for enhancing the adsorptive capacity of a molecular sieve according to claim 2 or 3, wherein: a flame arrester (10) is arranged on the evacuation pipeline (400), and the flame arrester (10) prevents sparks in a fire cabinet from channeling into the evacuation pipeline (400) to generate deflagration.
5. The treatment system for enhancing the adsorptive capacity of a molecular sieve of claim 4, wherein: a regeneration gas discharge pipeline (800) is connected between the evacuation pipeline (400) and the regeneration gas supply pipeline (500), a discharge program control valve (6) is arranged on the regeneration gas discharge pipeline (800), and a signal input end of the discharge program control valve (6) is connected with a central control DCS system.
6. A treatment system for enhancing the adsorptive capacity of a molecular sieve according to claim 5, wherein: a second check valve (9) is arranged on the regenerated gas discharge pipeline (800), and the second check valve (9) is used for preventing regenerated gas between the emptying pipeline (400) and the regenerated gas supply pipeline (500) from channeling, so that the safe operation of the treatment system is ensured.
7. A treatment system for enhancing the adsorption capacity of a molecular sieve according to any one of claims 1 to 3 or 5 to 6, wherein: the regenerated gas control pipeline (700) is provided with a first check valve (8), and the first check valve (8) is used for preventing regenerated gas between the regenerated cold blowing circulation pipeline (600) and the regenerated gas control pipeline (700) from channeling, so that safe operation of a treatment system is ensured.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN119656789A (en) * | 2024-11-29 | 2025-03-21 | 国家能源集团宁夏煤业有限责任公司 | Air separation device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN119656789A (en) * | 2024-11-29 | 2025-03-21 | 国家能源集团宁夏煤业有限责任公司 | Air separation device |
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