CN213771865U - Double-stage double-separation parallel synergistic methanol production system - Google Patents
Double-stage double-separation parallel synergistic methanol production system Download PDFInfo
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- CN213771865U CN213771865U CN202021868147.XU CN202021868147U CN213771865U CN 213771865 U CN213771865 U CN 213771865U CN 202021868147 U CN202021868147 U CN 202021868147U CN 213771865 U CN213771865 U CN 213771865U
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Abstract
The utility model discloses a two-stage double-separation parallel synergistic methanol production system, which comprises a first reactor, a second reactor, a first heat exchanger, a second heat exchanger, a first separation tank, a second separation tank and a compressor; the first reactor is communicated with an air inlet of a compressor after passing through a first heat exchanger and a first separation tank; the second reactor is communicated with the air inlet of the compressor after passing through the second heat exchanger and the second separation tank; an exhaust port of the compressor is respectively communicated with the first reactor and the second reactor through the first heat exchanger and the second heat exchanger through two branch pipes, and the raw material pipe is communicated with the two branch pipes; the first steam pocket is communicated with a refrigerant inlet of the first reactor, and the second steam pocket is communicated with the second reactor. By using the method and the device, the process flow can be set simply and reasonably, the equipment investment is reduced, the circulating power consumption is reduced, and the steam yield is high.
Description
Technical Field
The utility model relates to a parallelly connected increase methyl alcohol production system of doublestage double separation.
Background
Methanol synthesis usually uses synthesis gas and hydrogen as raw materials to synthesize, then the reaction mixed gas discharged from a reactor passes through a gas-liquid separator, methanol condensed in the gas-liquid separator is separated, unreacted gas separated by the gas-liquid separator is returned to the reactor to continue reaction, and fresh synthesis gas called make-up gas is supplemented to a reaction system to continue reaction, in the production process, in order to improve reaction efficiency, a multistage reactor is generally adopted, and fresh synthesis gas is continuously supplemented to a first stage reactor, in the reaction system, a last stage reactor is generally carried out in a self-circulation mode, reactors with different gas concentrations are required to be arranged, the types of the reactors are increased, not only is the maintenance cost of the reactors increased, but also different control modes and control points are required to be adopted due to the reactors with different forms, the difficulty of production stability is also increased.
SUMMERY OF THE UTILITY MODEL
In order to solve the problems, the utility model provides a two-stage double-separation parallel synergistic methanol production system, which comprises a first reactor, a second reactor, a first heat exchanger, a second heat exchanger, a first separation tank, a second separation tank and a compressor;
a first discharge hole of the first reactor is communicated with an inlet of a heat medium channel of the first heat exchanger, an outlet of the heat medium channel of the first heat exchanger is communicated with a first material inlet of the first separation tank through a first mixed gas pipe, and a first gas outlet of the first separation tank is communicated with a gas inlet of the compressor;
a second discharge hole of the second reactor is communicated with an inlet of a heating medium channel of the second heat exchanger, an outlet of the heating medium channel of the second heat exchanger is communicated with a second material inlet of the second separation tank through a second mixed gas pipe, and a second gas outlet of the second separation tank is communicated with a gas inlet of the compressor;
two branch pipes are led out from an exhaust port of the compressor and are respectively a first lean gas branch pipe and a second lean gas branch pipe, wherein the first lean gas branch pipe is connected to an inlet of a refrigerant channel of the first heat exchanger, and an outlet of the refrigerant channel of the first heat exchanger is communicated with a first feed inlet of the first reactor; the second lean gas branch pipe is connected to an inlet of a refrigerant channel of the second heat exchanger, and an outlet of the refrigerant channel of the second heat exchanger is communicated with a second feed inlet of the second reactor;
the raw material pipe is communicated with the first lean gas pipe and the second lean gas pipe;
a first liquid discharge port for discharging liquid methanol is arranged at the bottom of the first separation tank, and a second liquid discharge port for discharging liquid methanol is arranged at the bottom of the second separation tank; a first cooler group is connected in series on the first mixed gas pipe, and a second cooler group is connected in series on the second mixed gas pipe;
a first lower water outlet of the first steam drum is communicated with a refrigerant inlet of the first reactor, and a first upper water outlet of the first steam drum is communicated with a refrigerant outlet of the first reactor; and a second descending water port of the second steam pocket is communicated with a refrigerant inlet of the second reactor, and a second ascending water port of the second steam pocket is communicated with a refrigerant outlet of the second reactor.
By using the method, the process flow can be set simply and reasonably, and the equipment investment is reduced; by adopting two reactors, the preparation of a compressor can be reduced, the use efficiency of the compressor is improved, and the work consumption of the circulating power is reduced; the heat in the methanol synthesis process can be quickly removed, medium-pressure steam is byproduct, the steam yield is high, the water circulation is solved by adopting a high-position steam drum natural circulation mode, no power consumption is caused, and the high-efficiency energy-saving requirement is met; fresh synthesis gas as make-up gas can be uniformly fed into the first reactor and the second reactor, and the loads of the two reactors can be effectively adjusted. A separation tank is arranged corresponding to each reactor, so that the device can be enlarged, and the content of methanol entering the tower can be reduced as much as possible. The concentration of the reaction gas is basically the same for each reactor, and the reaction gas can be controlled by approximately the same parameters, so that the stability of process control is effectively improved.
In particular, the first reactor and the second reactor are both radial reactors. The radial reactor is a centrifugal radial reactor, a centripetal radial reactor or a centrifugal-centripetal radial reactor. The radial reactor has the advantages of uniform gas distribution and low bed resistance, and can effectively reduce the energy consumption during reaction. By centrifugal radial reactor is meant that the synthesis gas enters from the centre of the reactor and flows radially outwards into the annulus surrounding the bed and then exits the reactor from the annulus. The radial reactor of the centripetal type means that synthesis gas firstly enters an annular space around a bed layer, then flows to the center of the reactor along the radial direction, enters an exhaust pipe at the center of the reactor and then flows out of the reactor through the exhaust pipe. The centrifugal-centripetal radial reactor is characterized in that synthesis gas firstly enters an air inlet pipe at the central part of the reactor, then flows outwards in the radial direction and enters an annular space, then flows downwards along the annular space, then flows inwards in the radial direction, enters an exhaust pipe at the central part of the reactor, and finally is discharged out of the reactor through the exhaust pipe, and the centrifugal-centripetal radial flow tubular water bed reactor with the application number of 201911333118.5 is the centrifugal-centripetal radial reactor.
Further, the first cooler group comprises a first air cooler and a first water cooler which are connected in series on the first mixed gas pipe, and the second cooler group comprises a second air cooler and a second water cooler which are connected in series on the second mixed gas pipe. The first water cooler is closer to the first separation tank than the first air cooler; the second water cooler is closer to the second separation tank than the second air cooler. The materials firstly pass through the air cooler, so that the temperature difference between the atmosphere and the materials can be fully utilized, and the water consumption of the water cooler is reduced, thereby reducing the whole production cost.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present invention.
Detailed Description
Referring to fig. 1, a two-stage double-separation parallel synergistic methanol production system includes a first reactor 11, a second reactor 21, a first heat exchanger 13, a second heat exchanger 23, a first separation tank 16, a second separation tank 26, and a compressor 31.
The first discharge port 112 of the first reactor 11 is communicated with the inlet of the heat medium channel of the first heat exchanger 13, the outlet of the heat medium channel of the first heat exchanger 13 is communicated with the first material inlet 161 of the first separation tank 16 through the first mixed gas pipe 131, and the first gas outlet 162 of the first separation tank 16 is communicated with the gas inlet of the compressor 31.
The second discharge port 212 of the second reactor 21 is communicated with the inlet of the heating medium channel of the second heat exchanger 23, the outlet of the heating medium channel of the second heat exchanger 23 is communicated with the second material inlet 261 of the second separation tank 26 through a second mixed gas pipe 231, and the second gas outlet 262 of the second separation tank 26 is communicated with the gas inlet of the compressor 31. The compressor in this embodiment is a turbine compressor.
Two branch pipes, namely a first lean gas branch pipe 17 and a second lean gas branch pipe 27, are led out from the exhaust port of the compressor, wherein the first lean gas branch pipe 17 is connected to the inlet of the refrigerant channel of the first heat exchanger 13, and the outlet of the refrigerant channel of the first heat exchanger 13 is communicated with the first feed port 111 of the first reactor 11. The second lean branch pipe 27 is connected to an inlet of a refrigerant channel of the second heat exchanger 23, and an outlet of the refrigerant channel of the second heat exchanger 23 communicates with the second feed port 211 of the second reactor 21.
The raw material pipe 41 is divided into two branch pipes, namely a first raw material branch pipe 42 and a second raw material branch pipe 43, wherein the first raw material branch pipe 42 is communicated with the first lean gas pipe 17, and the second raw material branch pipe 43 is communicated with the second lean gas pipe 27.
A first drain port 163 for discharging liquid methanol is provided in the bottom of the first separation tank 16, and a second drain port 263 for discharging liquid methanol is provided in the bottom of the second separation tank.
An exhaust pipe 271 is installed on the second gas outlet 262, and the exhaust pipe 271 is used for discharging part of the gas discharged from the second separation tank to reduce the concentration of the non-condensable gas in the system, and the discharged gas is subjected to hydrogen recovery.
A first cooler group is connected in series to the first mixed gas pipe 131, and in this embodiment, the first cooler group includes a first air cooler 14 and a first water cooler 15 connected in series to the first mixed gas pipe 131, and the first water cooler 15 is located closer to the first separation tank 16 than the first air cooler 14.
A second cooler group is connected in series to the second mixed gas pipe 231; in this embodiment, the second cooler group includes a second air cooler 24 and a second water cooler 25 connected in series to the second mixed gas pipe 231, and the second water cooler 25 is located closer to the second separation tank 26 than the second air cooler 24.
The first lower water drop port 121 of the first steam drum 12 is communicated with the refrigerant inlet 113 of the first reactor 11, and the first upper water drop port 122 of the first steam drum 12 is communicated with the refrigerant outlet 114 of the first reactor. And a first steam discharge port 123 is provided at the top of the first drum 12, and a first water inlet port 124 and a first drain pipe 125 are provided at the bottom of the first drum.
The second falling water port 221 of the second drum 22 is communicated with the refrigerant inlet 213 of the second reactor 21, and the second rising water port 222 of the second drum 22 is communicated with the refrigerant outlet 214 of the second reactor. And a second steam discharge port 223 is provided at the top of the second drum 22, and a second water inlet 224 and a second soil discharge pipe 225 are provided at the bottom of the second drum.
In this example, the first reactor and the second reactor are both radial reactors, and the first reactor and the second reactor are both centrifugal-centripetal radial reactors. It is understood that in other embodiments, the first reactor and the second reactor may also be both centrifugal radial reactors, radial reactors of the radial type.
Claims (6)
1. The double-stage double-separation parallel synergistic methanol production system is characterized by comprising a first reactor, a second reactor, a first heat exchanger, a second heat exchanger, a first separation tank, a second separation tank and a compressor;
a first discharge hole of the first reactor is communicated with an inlet of a heat medium channel of the first heat exchanger, an outlet of the heat medium channel of the first heat exchanger is communicated with a first material inlet of the first separation tank through a first mixed gas pipe, and a first gas outlet of the first separation tank is communicated with a gas inlet of the compressor;
a second discharge hole of the second reactor is communicated with an inlet of a heating medium channel of the second heat exchanger, an outlet of the heating medium channel of the second heat exchanger is communicated with a second material inlet of the second separation tank through a second mixed gas pipe, and a second gas outlet of the second separation tank is communicated with a gas inlet of the compressor;
two branch pipes are led out from an exhaust port of the compressor and are respectively a first lean gas branch pipe and a second lean gas branch pipe, wherein the first lean gas branch pipe is connected to an inlet of a refrigerant channel of the first heat exchanger, and an outlet of the refrigerant channel of the first heat exchanger is communicated with a first feed inlet of the first reactor; the second lean gas branch pipe is connected to an inlet of a refrigerant channel of the second heat exchanger, and an outlet of the refrigerant channel of the second heat exchanger is communicated with a second feed inlet of the second reactor;
the raw material pipe is communicated with the first lean gas pipe and the second lean gas pipe;
a first liquid discharge port for discharging liquid methanol is arranged at the bottom of the first separation tank, and a second liquid discharge port for discharging liquid methanol is arranged at the bottom of the second separation tank; a first cooler group is connected in series on the first mixed gas pipe, and a second cooler group is connected in series on the second mixed gas pipe;
a first lower water outlet of the first steam drum is communicated with a refrigerant inlet of the first reactor, and a first upper water outlet of the first steam drum is communicated with a refrigerant outlet of the first reactor; and a second descending water port of the second steam pocket is communicated with a refrigerant inlet of the second reactor, and a second ascending water port of the second steam pocket is communicated with a refrigerant outlet of the second reactor.
2. The two-stage dual-separation parallel synergistic methanol production system of claim 1, wherein,
the first reactor and the second reactor are both radial reactors.
3. The two-stage dual-separation parallel synergistic methanol production system of claim 2, wherein,
the radial reactor is a centrifugal radial reactor, a centripetal radial reactor or a centrifugal-centripetal radial reactor.
4. The two-stage dual-separation parallel synergistic methanol production system of claim 1, wherein,
the compressor is a turbine compressor.
5. The two-stage dual-separation parallel synergistic methanol production system of claim 1, wherein,
the first cooler group comprises a first air cooler and a first water cooler which are connected in series on a first mixed gas pipe, and the second cooler group comprises a second air cooler and a second water cooler which are connected in series on a second mixed gas pipe.
6. The dual stage dual separation parallel enhanced methanol production system of claim 5 wherein the first water cooler is closer to the first separation tank than the first air cooler; the second water cooler is closer to the second separation tank than the second air cooler.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202021868147.XU CN213771865U (en) | 2020-08-31 | 2020-08-31 | Double-stage double-separation parallel synergistic methanol production system |
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| CN202021868147.XU CN213771865U (en) | 2020-08-31 | 2020-08-31 | Double-stage double-separation parallel synergistic methanol production system |
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