CN213556196U - Raw material air purification system of air separation equipment - Google Patents
Raw material air purification system of air separation equipment Download PDFInfo
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- CN213556196U CN213556196U CN202021889704.6U CN202021889704U CN213556196U CN 213556196 U CN213556196 U CN 213556196U CN 202021889704 U CN202021889704 U CN 202021889704U CN 213556196 U CN213556196 U CN 213556196U
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Abstract
A raw material air purification system of air separation equipment comprises a cold box, a nitrogen water precooling system, a pressure relief electric regulating valve, a controller, two adsorbers and two pressure sensors, wherein the top of each adsorber is respectively connected with the cold box and regeneration gas through two stop valves, and the bottom of each adsorber is respectively connected with the nitrogen water precooling system and a diffusion pipeline through two stop valves; the pressure relief electric control valve is installed on the relief pipeline and connected with an output port of the controller, and the first pressure sensor and the second pressure sensor are installed on pipelines at two ends of the pressure relief electric control valve and connected with different input ports of the controller. The utility model discloses utilize pressure sensor real-time measurement governing valve both sides atmospheric pressure, the controller makes governing valve both sides pressure differential according to setting for the curvilinear motion according to governing valve both sides pressure differential accurate control electric control valve's aperture, when guaranteeing pressure release speed, prevents that the adsorber from because of the pressure dip impaired to the safety of adsorber has been guaranteed, has improved work efficiency.
Description
Technical Field
The utility model relates to an air separation equipment (air separation plant) for drive the purification system of moisture, carbon dioxide and most hydrocarbon in the air separation, belong to separation technical field.
Background
The 'purification system' is an important component of the sixth generation of air separation equipment, and has the core functions of: the selective adsorption characteristic of the adsorbent in the purification system is utilized to remove moisture (dew point is less than or equal to-65 ℃), carbon dioxide (less than 1ppm) and most of hydrocarbon in the raw air.
A horizontal double-layer bed structure in a purification system of a mainstream air separation unit consists of two adsorber tanks (hereinafter referred to as adsorbers), wherein the upper layer in each adsorber is filled with a molecular sieve adsorbent (for adsorbing carbon dioxide and hydrocarbon in air); the lower layer is filled with active alumina adsorbent (adsorbing water in the air). When the device works, raw material air passes through the adsorbent from bottom to top in the adsorber to complete adsorption and removal of moisture, carbon dioxide and most of hydrocarbons. During regeneration, heated sewage nitrogen passes through the adsorbent from top to bottom to complete desorption and regeneration, one adsorber generally performs normal adsorption work, the other adsorber performs regeneration (including pressure relief, heating and cold blowing), and the two adsorbers are alternately used, so that the requirement of continuous operation of the air separation equipment is met.
The core working substance of the "purification system" is adsorbent (activated alumina and molecular sieve), which is porous and has certain strength, and the adsorption is completed by the adsorbed component with diameter smaller than the hole diameter in the adsorbent and sucked into the inside of the hole, and the gas molecules larger than the hole diameter are blocked outside the hole and are not adsorbed. The adsorption process is an exothermic process, and macroscopically appears as: the temperature of the raw material air outlet adsorber is higher than that of the inlet; in contrast: warming during regeneration (desorption) is an endothermic process. Because the capacity of the adsorbent for adsorbing the adsorbed components is increased along with the increase of the partial pressure of the adsorbed components at a certain adsorption working temperature, the adsorbent for adsorbing and saturating the adsorbed components is adsorbed at a higher working pressure (0.48Mpa), a large amount of adsorbed components are analyzed due to the reduction of the partial pressure of the adsorbed components outside the adsorbent after pressure relief, and because the analysis process is an endothermic process, the temperature of the adsorbent in the regenerated adsorber is sharply reduced (can reach below minus 7 ℃) after the pressure of the regenerated adsorber is relieved to the normal pressure.
After the adsorbent adsorbs the saturated adsorbed component, the adsorption capacity is lost. Measures must be taken to drive the adsorbed component away from the adsorbent surface and restore the adsorbent's adsorption capacity, a process known as "regeneration". Firstly, utilizing the principle of that adsorption capacity of adsorbent is reduced at high temp., introducing heating gas into adsorbent layer to raise temp. of adsorbent, and making adsorbed component be resolved, then utilizing the heating gas to carry out adsorption, and said method is called heating regeneration or heat-exchange regeneration. The other regeneration is pressure reduction regeneration or pressure alternation regeneration, the pressure in the adsorber is reduced during regeneration, even the adsorber is vacuumized, so that the partial pressure of the adsorbed component is reduced, the concentration of the adsorbed component is reduced, the number of molecules adsorbed on the surface of the adsorbent is correspondingly reduced, and the aim of regeneration is fulfilled. The regeneration gas of the adsorption system is waste nitrogen (the oxygen content is 2-3%, the rest contains a small amount of argon and most of nitrogen) separated from the middle upper part of an upper tower of the air separation system, the waste nitrogen is reheated by a subcooler and a main heat exchanger after coming out of the upper tower and then is discharged out of a cooling box at the temperature of about 12-15 ℃, the waste nitrogen with the pressure of about 10Kpa is discharged out of the cooling box and then is divided into two parts, one part enters a nitrogen water precooling system to carry out preliminary cooling on chilled water; the other strand enters a purification system to carry out desorption regeneration on the adsorbent which adsorbs saturated adsorbed components and is decompressed to normal pressure, the general desorption regeneration process is that firstly an electric heater is used for heating the waste nitrogen to 180-plus-200 ℃, then the high-temperature waste nitrogen is introduced into an adsorbent bed layer to heat the adsorbent, the electric heater is stopped after being started for a period of time (the temperature of the outlet of the heated adsorber is more than 20 ℃), the cold blowing cooling is carried out on the heated adsorbent at the heating inlet by using the normal-temperature waste nitrogen to recover the capacity of the adsorbent for adsorbing the adsorbed components, and meanwhile, the heat storage capacity when the electric heater of the adsorbent bed layer is started is continuously used for heating the waste nitrogen to the adsorbent at the outlet until the adsorbent bed layer is completely subjected to the process of more than 140 ℃ once and is recovered to the normal temperature (less than 25 ℃).
The pressure release process is required to be carried out before the pressure reduction and regeneration of the adsorber, in order to improve the working efficiency, the pressure release process is as short as possible, when the pressure release speed is too high, the pressure in the adsorber suddenly drops, high-pressure gas is sprayed out rapidly, part of adsorbent falls off and is blown out by high-speed airflow, the adsorber is damaged, the fallen adsorbent can block a gas pipeline, and the purification system cannot normally run. At present, the pressure relief process of the adsorber is mainly controlled by a manual regulating valve, the control effect is greatly influenced by human factors, the requirement on the technical level of operators is high, and the safety of the adsorber cannot be ensured, so that the problem that how to accurately control the pressure relief speed of the adsorber always puzzles related technical personnel is solved.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide an air separation equipment's raw materials air purification system to the drawback of prior art to improve the control accuracy of adsorber pressure release process, when guaranteeing adsorber safety, shorten the pressure release time, improve work efficiency.
The problem of the utility model is solved with following technical scheme:
a raw material air purification system of air separation equipment comprises a cold box, a nitrogen water precooling system, a pressure relief electric regulating valve, a controller, two adsorbers and two pressure sensors, wherein the top of each adsorber is respectively connected with the cold box and regeneration gas through two stop valves, and the bottom of each adsorber is respectively connected with the nitrogen water precooling system and a diffusion pipeline through two stop valves; the pressure relief electric control valve is installed on the relief pipeline and connected with an output port of the controller, and the first pressure sensor and the second pressure sensor are installed on pipelines at two ends of the pressure relief electric control valve and connected with different input ports of the controller.
The raw material air purification system of the air separation equipment further comprises a pressure-equalizing electric regulating valve, a third pressure sensor and a fourth pressure sensor, wherein the pressure-equalizing electric regulating valve is installed between top connectors of the two adsorbers, the control end of the pressure-equalizing electric regulating valve is connected with the output port of the controller, and the third pressure sensor and the fourth pressure sensor are installed on pipelines at two ends of the pressure-equalizing electric regulating valve and are connected with different input ports of the controller.
In the raw material air purification system of the air separation equipment, the regeneration gas is waste nitrogen separated from the upper middle part of the upper tower of the air separation system, and an electric heater is arranged on a conveying pipeline of the waste nitrogen.
In the raw material air purification system of the air separation equipment, the electric heater is provided with the inlet stop valve and the bypass stop valve.
In the raw material air purification system of the air separation equipment, the tail end of the diffusing pipeline is provided with the emptying silencer.
In the raw material air purification system of the air separation plant, the controller is a PID controller.
The utility model discloses utilize pressure sensor real-time measurement governing valve both sides atmospheric pressure, the controller makes governing valve both sides pressure differential according to setting for the curvilinear motion according to governing valve both sides pressure differential accurate control electric control valve's aperture, when guaranteeing pressure release speed, prevents that the adsorber from because of the pressure dip impaired to the safety of adsorber has been guaranteed, has improved work efficiency.
Drawings
The present invention will be described in detail with reference to the accompanying drawings.
Fig. 1 is a schematic structural diagram of the present invention;
FIG. 2 is a state of operation of the first adsorber during regeneration of the second adsorber;
FIG. 3 is a state when the first adsorber is pressurized;
FIG. 4 is a state of operation of the first adsorber in parallel with the second adsorber;
FIG. 5 is a state during pressure relief of the second adsorber;
FIG. 6 is a state of operation of the second adsorber during regeneration of the first adsorber.
Description of the drawings: in the above figures, the thin solid line indicates a gas-free flow line, the thick solid line indicates a raw material air flow path, the thick two-dot chain line indicates a dirty nitrogen flow path, and the broken line indicates a wire.
In the drawings, the reference numerals denote: 1. the system comprises an electric heater, a cooling box, a nitrogen water precooling system, a vent muffler, an FS1, a first adsorber, an FS2, a second adsorber, P1-P4, first-fourth pressure sensors, F1-F10, first-tenth stop valves, DF1, a pressure relief electric regulating valve, a DF2, a pressure equalizing electric regulating valve, a U1 and a controller.
Detailed Description
Referring to fig. 1, the utility model discloses including electric heater 1, cold box 2, nitrogen water precooling system 3, emptying silencer 4, controller U1, pressure release electrical control valve DF1, voltage-sharing electrical control valve DF2, two adsorbers (namely first adsorber FS1 and second adsorber FS2), four pressure sensors (namely first pressure sensor P1-fourth pressure sensor P4) and ten stop valves (namely first stop valve F1-tenth stop valve F10), the top of first adsorber FS1 is connected with cold box 2 and regeneration gas pipeline respectively through first stop valve F1 and second stop valve F2, the bottom is connected with nitrogen water precooling system 3 and diffusion pipeline respectively through third stop valve F3 and fourth stop valve F4; the top of the second adsorber FS2 is respectively connected with the cold box 2 and the regeneration gas pipeline through a fifth stop valve F5 and a sixth stop valve F6, and the bottom of the second adsorber is respectively connected with the nitrogen water precooling system 3 and the diffusing pipeline through a seventh stop valve F7 and an eighth stop valve F8; the pressure relief electric control valve DF1 is installed on a relief pipeline and connected with an output port of the controller U1, and the first pressure sensor P1 and the second pressure sensor P2 are respectively installed at two ends of the pressure relief electric control valve DF1 and connected with an input port of the controller U1. The pressure equalizing electric regulating valve DF2 is installed between the top connectors of the two adsorbers, the control end of the pressure equalizing electric regulating valve DF2 is connected with the output port of the controller U1, and the third pressure sensor P3 and the fourth pressure sensor P4 are installed on the pipelines at the two ends of the pressure equalizing electric regulating valve DF2 and are connected with different input ports of the controller U1. The regeneration gas is the dirty nitrogen gas that the upper middle part of tower separation was gone up to the air separation system, and electric heater 1 installs on the pipeline of dirty nitrogen gas. The ninth cut-off valve F9 is an inlet cut-off valve of the electric heater 1, and the tenth cut-off valve F10 is a bypass cut-off valve of the electric heater 1. The vent muffler 4 is installed at the end of the vent line. The controller U1 adopts PID controller, and can select iSeries series PID controller.
The purification system works as follows:
assuming that the first adsorber FS1 is in a regeneration state, the second adsorber FS2 is in an operating state, and the raw air and dirty nitrogen flow paths are as shown in fig. 2, the first cut-off valve F1, the third cut-off valve F3, the sixth cut-off valve F6, and the eighth cut-off valve F8 are closed, the remaining cut-off valves are opened, the pressure-reducing electric control valve DF1 is in an operating state, and the pressure-equalizing electric control valve DF2 is closed. The working process of the purification system comprises five steps of pressurizing, parallel connection, pressure relief, heating and cold blowing.
Switching process of the first adsorber FS1 after cold blowing:
pressurizing: a second cut-off valve F2 and a fourth cut-off valve F4; the controller U1 slowly opens (14-20 minutes) the pressure equalizing electric control valve DF2 to charge the first adsorber FS1 to be used, and closes the pressure equalizing electric control valve DF2 after the pressures of the two adsorbers are consistent (0.47 Mpa); the method comprises the steps that a pressure equalizing electric regulating valve DF2 is utilized to divide a part of clean raw material air from a second adsorber FS2 in normal adsorption work to charge and boost the pressure of the regenerated first adsorber FS1, so as to prepare for the normal use of the first adsorber FS 1; before pressurizing: the pressure is basically 0, the inlet temperature is 10-14 ℃, and the outlet temperature is less than 25 ℃; after pressurization: the pressure is 0.47Mpa, the inlet temperature is 8-12 deg.C, the outlet temperature is above 30 deg.C, and then slowly cooling to 12-16 deg.C and stabilizing. The dirty nitrogen line is closed during charging and the flow path of the raw air is shown in fig. 3.
Parallel connection: the first stop valve F1 and the third stop valve F3 are opened in parallel for 1 minute; in the step, the first adsorber FS1 and the second adsorber FS2 are used together in parallel, whether the adsorption work of the first adsorber FS1 is normal or not is observed, the first adsorber FS1 is prepared for being used alone, a waste nitrogen pipeline is closed in the parallel connection process, and the flow path of raw material air is shown in figure 4.
Pressure relief: the fifth cut-off valve F5 and the seventh cut-off valve F7 are closed, the eighth cut-off valve F8 is opened after one minute, the second adsorber FS2 is depressurized (generally for 11 to 15 minutes) by the depressurization electric control valve DF1, and the depressurization speed is controlled by the depressurization electric control valve DF1 (as shown in fig. 5). When the pressure of the second adsorber FS2 is close to 0, a sixth stop valve F6 is opened to introduce the dirty nitrogen, at the moment, a pressure relief electric regulating valve DF1 is fully opened, and the flow paths of the raw material air and the dirty nitrogen are shown in FIG. 6; discharging pressure raw material air which is used for adsorbing saturated water, carbon dioxide and most of hydrocarbons when the second adsorber FS2 works through an eighth stop valve F8 and a pressure relief electric regulating valve DF1 to prepare for the regeneration of the second adsorber FS 2; before pressure relief: the pressure is 0.47Mpa, the inlet temperature is 8-12 ℃, the outlet temperature is about 12-16 ℃, and after pressure relief: the pressure is 0Mpa, the inlet temperature is 10-14 ℃, and the outlet temperature is about 0 ℃.
Heating: one minute later, the electric heater 1 was activated to warm-up and regenerate the second adsorber FS2 (raw air and dirty nitrogen flow path unchanged); the method comprises the steps of heating low-pressure sewage nitrogen (the pressure is less than 5kpa, the temperature is 10-14 ℃) and raising the temperature (180-; before heating: heating under 0Mpa at inlet temperature of 10-14 deg.C and outlet temperature of 0 deg.C: the pressure is 0Mpa, the inlet temperature is 180-.
Cold blowing: the flow paths of the raw material air and the waste nitrogen are unchanged, the electric heater 1 is powered off after being started for a period of time (103 minutes for Xinda oxygen generation 4# unit) and the outlet temperature of the second adsorber FS2 is higher than 20 ℃, the heating is stopped, cold blowing is switched, and the next switching period is started when the temperature of the cold blowing is 230 minutes and the temperature of the waste nitrogen out of the adsorber is reduced from the highest temperature of higher than 140 ℃ to lower than 25 ℃. The method comprises the steps of firstly, continuously heating and regenerating the adsorbent which is not heated by the heat storage capacity in the adsorber when the electric heater is started, and then, cold blowing the high-temperature adsorbent to the normal temperature by using normal-temperature sewage nitrogen to recover the adsorption capacity for later use. Before cold blowing: pressure 0Mpa, inlet temperature 180-: the pressure is 0Mpa, the inlet temperature is 10-14 ℃, the outlet temperature is more than 140 ℃ at most, and the temperature reaches below 25 ℃ after the cold blowing is finished.
Cold-blow-completed switching process of the second adsorber FS 2:
pressurizing: a sixth cut-off valve F6 and a closed eighth cut-off valve F8; the controller U1 makes the pressure equalizing electric control valve DF2 open slowly (14-20 minutes) to charge the pressure of the second adsorber FS2 to be used, and closes the pressure equalizing electric control valve DF2 after the pressures of the two adsorbers are consistent (0.47 Mpa); the method comprises the steps that a pressure equalizing electric regulating valve DF2 is utilized to divide a part of clean raw material air from a first adsorber FS1 in normal adsorption work to charge and boost the pressure of a second adsorber FS2 which is completely regenerated, so that preparation is made for the second adsorber FS2 to be put into normal use; before pressurizing: the pressure is basically 0, the inlet temperature is 10-14 ℃, and the outlet temperature is less than 25 ℃; after pressurization: the pressure is 0.47Mpa, the inlet temperature is 8-12 deg.C, the outlet temperature is above 30 deg.C, and then slowly cooling to 12-16 deg.C and stabilizing. And closing the waste nitrogen pipeline in the pressurizing process.
Parallel connection: the fifth stop valve F5 and the seventh stop valve F7 are opened in parallel for 1 minute; in the step, the first adsorber FS1 and the second adsorber FS2 are used in parallel, whether the adsorption work of the second adsorber FS2 is normal or not is observed, preparation is made for the independent use of the second adsorber FS2, and a waste nitrogen pipeline is closed in the parallel connection process.
Pressure relief: the first shut-off valve F1 and the third shut-off valve F3 are closed, the fourth shut-off valve F4 is opened after one minute, and the first adsorber FS1 is depressurized (generally for 11 to 15 minutes) by the depressurization electric control valve DF1, with the depressurization speed being controlled by the depressurization electric control valve DF 1. When the pressure of the first adsorber FS1 is close to 0, opening a second stop valve F2 to introduce the polluted nitrogen, and fully opening a pressure relief electric regulating valve DF1 at the moment; the method comprises the following steps that pressure raw material air generated when a first adsorber FS1 absorbing saturated water, carbon dioxide and most of hydrocarbons works is discharged through a fourth stop valve F4 and a pressure relief electric control valve DF1, and preparation is made for regeneration of the first adsorber FS 1; before pressure relief: the pressure is 0.47Mpa, the inlet temperature is 8-12 ℃, the outlet temperature is about 12-16 ℃, and after pressure relief: the pressure is 0Mpa, the inlet temperature is 10-14 ℃, and the outlet temperature is about 0 ℃.
Heating: after one minute, the electric heater 1 is started to heat and regenerate the first adsorber FS1 (the raw air and the waste nitrogen flow path are unchanged); the method comprises the steps of heating low-pressure sewage nitrogen (the pressure is less than 5kpa, the temperature is 10-14 ℃) and raising the temperature (180-; before heating: heating under 0Mpa at inlet temperature of 10-14 deg.C and outlet temperature of 0 deg.C: the pressure is 0Mpa, the inlet temperature is 180-.
Cold blowing: the flow paths of the raw material air and the waste nitrogen are unchanged, the electric heater 1 is powered off after being started for a period of time (103 minutes for Xinda oxygen generation 4# unit) and the outlet temperature of the first adsorber FS1 is higher than 20 ℃, the heating is stopped and the cold blowing is switched, and the next switching period is started after the cold blowing is carried out for 230 minutes and the temperature of the waste nitrogen out of the adsorber is reduced from the highest temperature of higher than 140 ℃ to lower than 25 ℃. The method comprises the steps of firstly, continuously heating and regenerating the adsorbent which is not heated by the heat storage capacity in the adsorber when the electric heater is started, and then, cold blowing the high-temperature adsorbent to the normal temperature by using normal-temperature sewage nitrogen to recover the adsorption capacity for later use. Before cold blowing: pressure 0Mpa, inlet temperature 180-: the pressure is 0Mpa, the inlet temperature is 10-14 ℃, the outlet temperature is more than 140 ℃ at most, and the temperature reaches below 25 ℃ after the cold blowing is finished.
Claims (6)
1. A raw material air purification system of air separation equipment is characterized by comprising a cold box (2), a nitrogen water precooling system (3), a pressure relief electric regulating valve (DF1), a controller (U1), two adsorbers and two pressure sensors, wherein the top of each adsorber is respectively connected with the cold box (2) and regeneration gas through two stop valves, and the bottom of each adsorber is respectively connected with the nitrogen water precooling system (3) and a diffusion pipeline through two stop valves; the pressure relief electric control valve (DF1) is installed on a relief pipeline and is connected with an output port of the controller (U1), and the first pressure sensor (P1) and the second pressure sensor (P2) are installed on pipelines at two ends of the pressure relief electric control valve (DF1) and are connected with different input ports of the controller (U1).
2. The raw air purification system of an air separation plant according to claim 1, further comprising a pressure equalizing electric regulating valve (DF2), a third pressure sensor (P3) and a fourth pressure sensor (P4), wherein the pressure equalizing electric regulating valve (DF2) is installed between top ports of the two adsorbers, a control end of the pressure equalizing electric regulating valve (DF2) is connected with an output port of the controller (U1), and the third pressure sensor (P3) and the fourth pressure sensor (P4) are installed on a pipeline at two ends of the pressure equalizing electric regulating valve (DF2) and are connected with different input ports of the controller (U1).
3. The raw air purification system of an air separation plant according to claim 1 or 2, wherein the regeneration gas is a waste nitrogen gas separated from the upper middle part of the upper tower of the air separation system, and an electric heater (1) is provided on a conveying pipeline of the waste nitrogen gas.
4. A raw air purification system for an air separation plant according to claim 3, characterized in that the electric heater (1) is provided with an inlet shut-off valve and a bypass shut-off valve.
5. A raw air purification system for an air separation plant according to claim 4, wherein the discharge line is terminated with a discharge muffler (4).
6. A feed air purification system for an air separation plant according to claim 5 wherein said controller (U1) is a PID controller.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202021889704.6U CN213556196U (en) | 2020-09-02 | 2020-09-02 | Raw material air purification system of air separation equipment |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202021889704.6U CN213556196U (en) | 2020-09-02 | 2020-09-02 | Raw material air purification system of air separation equipment |
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| CN213556196U true CN213556196U (en) | 2021-06-29 |
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