CN216756375U - Energy-saving or yield-increasing and consumption-reducing methanol synthesis device - Google Patents

Abstract

The utility model discloses an energy-saving or yield-increasing and consumption-reducing methanol synthesis device, which comprises a methanol synthesis loop, wherein the methanol synthesis loop comprises a first methanol synthesis tower. Compared with the traditional methanol synthesis loop, the utility model can improve the alcohol net value, reduce the fresh gas unit consumption and reduce the energy consumption of the whole workshop section for newly-built synthesis devices; the reformed methanol device can solve the bottleneck of possible leakage or insufficient productivity of the methanol synthesis tower, increase the yield of the methanol and simultaneously realize energy conservation and consumption reduction.

Description

Energy-saving or yield-increasing and consumption-reducing methanol synthesis device

Technical Field

The utility model relates to the technical field of methanol synthesis, in particular to a methanol synthesis device which takes coal/natural gas/coke oven gas as raw materials and is energy-saving or capable of increasing yield and reducing consumption.

Background

The method aims at solving the problems of high energy consumption, insufficient capacity or other potential safety hazards and the like possibly existing in the conventional device by digging capacity, modifying and upgrading the existing device, is an important means for improving enterprise benefits, reducing comprehensive energy consumption, reducing production cost and improving long-period stable operation of the device, is one of effective methods for replacing high benefits with lower investment, and is also a way for enterprises to respond to national calls and fulfill self social responsibility.

At present, domestic methanol synthesis devices using coal as a raw material are numerous, but the economic benefit of the devices mainly depends on the prices of the raw material coal and the product methanol, so the comprehensive energy consumption basically determines the market competitiveness of the product.

With the continuous deepening of the policy of 'double reduction' in China, a large-scale coal chemical device is not built any more basically, how to utilize original equipment as much as possible, reduce energy consumption, increase productivity and increase the economic benefit of products is a difficult problem which must be faced when a methanol device can survive.

At present, the methanol production process selected by some domestic methanol enterprises is long-term, the design is outdated, the energy consumption is high, the efficiency is low, and a production device, particularly a methanol synthesis tower, has a serious production bottleneck and cannot meet the requirements of energy conservation and yield increase. Some methanol synthesis towers even have leakage hidden trouble, have very big safety risk, lead to many devices can't reach design productivity. In order to continuously update methanol technology, help the enterprises to upgrade and upgrade, improve energy efficiency, a plurality of modification methods for methanol loops are available on the market, and the energy-saving/yield-increasing modes are generally adopted as follows:

(1) one set of methanol synthesis loop is connected in parallel

The method saves energy/increases production by directly connecting a set of methanol loop in parallel, has large investment and large occupied area, and is not an optimal transformation means.

(2) Replacing a new synthesis tower or replacing new tower internals.

The new synthesis tower is replaced without completely utilizing the capacity of the existing device, the investment is large, the occupied area is large, and the simple and rough reconstruction means can not be accepted by enterprises generally. As for the scheme of replacing the tower internals, the device can be implemented after being completely stopped, the workload of field modification is large, the long-period operation of the device can be greatly influenced, and the economic benefit of the device is finally influenced.

SUMMERY OF THE UTILITY MODEL

The utility model aims to provide an energy-saving or yield-increasing and consumption-reducing methanol synthesis device by using a universal, energy-saving and small equipment investment method to help the existing methanol device loop to perform energy-saving/yield-increasing transformation and simultaneously solve the potential safety hazard possibly existing in the existing device. The energy-saving or yield-increasing and consumption-reducing methanol synthesis device can improve the conversion per pass and the net value of methanol to the maximum extent, obviously reduce the circulation ratio, and realize the purpose that the device reduces the comprehensive energy consumption or achieves the yield increase.

In order to achieve the above object, the energy-saving or yield-increasing and consumption-reducing methanol synthesis apparatus of the present invention comprises a methanol synthesis loop, wherein the methanol synthesis loop comprises a first methanol synthesis tower, and is characterized in that a second methanol synthesis tower is additionally provided, wherein the first methanol synthesis tower and the second methanol synthesis tower are connected in series, in series-parallel or in parallel.

In a preferred embodiment of the utility model, a fresh gas compressor, a recycle gas compressor and a gas heat exchanger are also included, the fresh gas compressor being connected on the one hand to the fresh gas via a first line and on the other hand to a second line; the circulating gas compressor is connected with a third pipeline, the second pipeline is connected with the third pipeline and then is connected with the gas-gas heat exchanger, the gas-gas heat exchanger is connected with a fifth pipeline through a fourth pipeline, the fifth pipeline is connected with the first methanol synthesis tower or the second methanol tower is connected, the first methanol tower or the second methanol tower is connected with the second methanol synthesis tower or the first methanol synthesis tower through a sixth pipeline, the fourth pipeline is further connected with the sixth pipeline, and the first methanol tower or the second methanol tower is connected with the gas-gas heat exchanger through a seventh pipeline.

In a preferred embodiment of the present invention, the second methanol synthesis column is disposed at the front side or the rear side of the first methanol synthesis column to specifically solve the practical problems of the prior art.

In a preferred embodiment of the present invention, the first methanol synthesis column is any type of reactor, and the second methanol synthesis column is an isothermal or adiabatic reactor; the isothermal reactor is of an axial structure or a radial structure; the adiabatic reactor is of an axial structure or a radial structure.

In a preferred embodiment of the present invention, the methanol synthesis system further comprises a first steam drum, the first steam drum is provided with a first steam-water mixture inlet and a first boiling water outlet, the first steam-water mixture inlet on the first steam drum is connected to the steam-water mixture outlet on the first methanol synthesis tower through a ninth pipeline, and the first boiling water outlet on the first steam drum is connected to the boiling water inlet on the first methanol synthesis tower through a tenth pipeline, so that the steam and water of the first methanol synthesis tower can naturally circulate.

In a preferred embodiment of the present invention, a pump is connected in series to the tenth line, and the pump forcibly circulates the boiling water in the first methanol synthesis column.

In a preferred embodiment of the utility model, the first steam drum is further provided with a first boiler feed water inlet, an intermediate pressure steam outlet and a first drain outlet, the first boiler feed water inlet is connected with boiler feed water through an eleventh pipeline, and the intermediate pressure steam outlet is connected with a steam pipe network through a twelfth pipeline; the first sewage discharge port is connected with a sewage discharge flash tank through a thirteenth pipeline; the eleventh pipeline and the tenth pipeline are connected through a valve.

In a preferred embodiment of the utility model, the methanol synthesis system further comprises a second steam drum, wherein a second steam-water mixture inlet and a second boiling water outlet are arranged on the second steam drum, the second steam-water mixture inlet on the second steam drum is connected with the steam-water mixture outlet on the second methanol synthesis tower through a fourteenth pipeline, and the second boiling water outlet on the second steam drum is connected with the boiling water inlet on the second methanol synthesis tower through a fifteenth pipeline, so that the steam-water natural circulation of the second methanol synthesis tower is facilitated; or the fourteenth pipeline and the fifteenth pipeline are connected with the first steam drum according to the actual working condition, and the second steam drum is eliminated.

In a preferred embodiment of the utility model, a saturated steam outlet, a second boiler feed water inlet and a second sewage outlet are further arranged on the second steam drum, and the saturated steam from the saturated steam outlet is sent out of the battery compartment through a sixteenth pipeline; the second boiler feed water inlet is connected with boiler feed water through a thirtieth pipeline, and the second sewage discharge outlet is connected with a sewage discharge flash tank through a thirty-first pipeline.

In a preferred embodiment of the utility model, the device further comprises a high-pressure methanol separator, a methanol flash tank and a purge gas washing tower, wherein the high-pressure methanol separator is provided with a methanol solution inlet, a separated gas outlet and a separated liquid outlet; a separated liquid inlet, a crude methanol outlet, a fuel gas outlet and a methanol solution backflow inlet are arranged on the methanol flash tank; the purge gas washing tower is provided with a washing water inlet, a separation gas inlet, a purge gas outlet and a methanol solution reflux outlet; a methanol solution inlet on the high-pressure methanol separator is connected with a methanol solution outlet on the gas-gas heat exchanger through a seventeenth pipeline and a water cooler, a separated gas outlet on the high-pressure methanol separator is connected with an inlet of a circulating gas compressor through an eighteenth pipeline on one hand, and is connected with a separated gas inlet on the purge gas washing tower through a nineteenth pipeline on the other hand, and the nineteenth pipeline is also connected with a torch through a twentieth pipeline; a separated liquid outlet on the high-pressure methanol separator is connected with a separated liquid inlet on the methanol flash tank through a twenty-one pipeline; the coarse methanol outlet on the methanol flash tank is connected with a downstream methanol rectification unit or an intermediate tank through a twenty-two pipeline, the fuel gas outlet on the methanol flash tank is connected with a torch through a twenty-three pipeline, the methanol solution reflux inlet on the methanol flash tank is connected with the methanol solution reflux outlet on the purge gas washing tower through a twenty-four pipeline, the washing high-pressure sealing water inlet on the purge gas washing tower is connected with washing water through a twenty-five pipeline, and the purge gas outlet on the purge gas washing tower is sent out of the battery compartment through a twenty-sixth pipeline.

Due to the adoption of the technical scheme, compared with the traditional methanol synthesis loop, the new synthesis device can improve the alcohol net value, reduce the unit consumption of fresh gas and reduce the energy consumption of the whole section; the reformed methanol device can solve the bottleneck of possible leakage or insufficient productivity of the methanol synthesis tower, increase the yield of methanol and simultaneously realize energy conservation and consumption reduction.

By the improvement of the existing methanol synthesis device, the utility model not only can reduce energy consumption and improve productivity by adopting lower investment, but also can relieve the operating environment of a reactor with defects (such as high hot spot temperature, easy leakage, incapability of operating at high load and the like), reduce the possibility of leakage of the reactor, and simultaneously improve the overall process performance of a synthesis loop, improve the quality of methanol products and improve the productivity by optimizing the operating conditions.

The utility model can be used for the yield increase transformation of the existing methanol production device, so that the yield increase amplitude of the existing methanol production device can reach 0-50%.

The utility model mainly connects a new synthesis tower in series/parallel on the basis of the original methanol loop to achieve the purpose of energy saving/yield increase.

Drawings

FIG. 1 is a schematic flow chart of an energy-saving or yield-increasing and consumption-reducing methanol synthesis plant according to example 1 of the present invention.

FIG. 2 is a schematic flow chart of an energy-saving or yield-increasing and consumption-reducing methanol synthesis plant according to embodiment 2 of the present invention.

Detailed Description

The utility model is further described below in conjunction with the appended drawings and detailed description.

The utility model mainly connects a new synthesis tower in series/parallel on the basis of the original methanol loop to achieve the purpose of energy saving/yield increase. Different flow configurations are designed for different demands of the yield-increasing target. For the improvement flow of the methanol synthesis loop with high hot spot temperature, easy leakage and incapability of high-load operation of the methanol synthesis tower, see the flow of the energy-saving or yield-increasing and consumption-reducing methanol synthesis device in the embodiment 1 shown in fig. 1; aiming at the problem that the design load of the original methanol synthesis tower is limited, and the methanol synthesis loop has the transformation process with the yield increase/energy saving requirement, the process of the methanol synthesis device which saves energy or increases the yield and reduces the consumption in the embodiment 2 shown in figure 2 is shown.

Example 1

Fresh gas enters a fresh gas compressor K through a first pipeline 1, the pressure of the fresh gas is increased to 7.5-8.0 MPa after the fresh gas is compressed by the fresh gas compressor K, the fresh gas is sent out from a second pipeline 2 to be mixed with circulating gas compressed by a circulating gas compressor J and sent out through a third pipeline 3, and the mixed gas is preheated to the temperature of 200-240 ℃ through a gas-gas heat exchanger E1 and is sent out through a fourth pipeline 4 as tower inlet gas. The mixed gas may be connected to the fourth line 4 via a twenty-seventh line 27 and a control valve 27a to control the temperature of the gas entering the column before it is preheated by the gas-gas heat exchanger E1.

The tower gas is divided into two paths, one path of tower gas firstly enters a second methanol tower R2 through a fifth pipeline 5 to react, the mixture of unreacted gas with the methanol concentration of 5-10 mol% and methanol steam formed by the reaction of the second methanol tower R2 flows out of the second methanol tower R2, is mixed with the other path of tower gas through a eighteenth pipeline 28, then enters a first methanol synthesis tower R1 through a sixth pipeline 6 to react, the methanol solution with the methanol concentration of 16-20 mol% formed by the reaction of the first methanol tower R1 flows into a gas-gas heat exchanger E1 through a seventh pipeline 7, and the mixed gas is preheated. In addition, the mixture of unreacted gas and methanol vapor having a methanol concentration of 5 to 10 mol% formed by the reaction in the second methanol column R2 may be further merged into the seventh line 7 through the twenty-ninth line 29.

The methanol from the methanol solution outlet of the gas-gas heat exchanger E1 is cooled to 40 ℃ through a seventeen pipeline 17 and a water cooler E2, and the cooled methanol solution enters a high-pressure methanol separator V3 through a methanol solution inlet on the high-pressure methanol separator V3 for gas-liquid separation.

The gas separated by the high-pressure methanol separator V3 flows out from the separated gas outlet of the high-pressure methanol separator V3, and one of the gas flows into the recycle gas compressor J as recycle gas through the eighteenth pipeline 18 connected with the inlet of the recycle gas compressor J to be compressed. The other stream is fed to the purge gas scrubber C1 via a nineteenth line 19 connected to the separated gas inlet of the purge gas scrubber C1 for purge and a twentieth line 20, which may also be connected to the nineteenth line 19, is fed to the flare as purge gas.

The twenty-first pipeline 21 connected with a separated liquid outlet on the liquid high-pressure methanol separator V3 and a separated liquid inlet on the methanol flash tank V4 after being separated by the high-pressure methanol separator V3 is sent into the methanol flash tank V4 for flash evaporation.

The crude methanol flashed in the methanol flash tank V4 flows out of the crude methanol outlet of the methanol flash tank V4 and is fed to the downstream methanol rectification unit or intermediate tank via a twenty-second line 22 connected to the downstream methanol rectification unit or intermediate tank.

The fuel gas flashed in the methanol flash drum V4 flows out through the fuel gas outlet on the methanol flash drum V4 and is sent to the flare for combustion through the twenty three lines 23 connected to the flare.

The separated gas entering the purge gas scrubber C1 is scrubbed by scrubbing water fed through the twenty-five line 25 and the scrubbing water inlet on the purge gas scrubber C1. The purge gas after washing by the purge gas scrubber C1 is taken out through the purge gas outlet of the purge gas scrubber C1 and sent out to the battery compartment through the twenty-sixth line 26 connected to the purge gas outlet of the purge gas scrubber C1.

The methanol solution washed by the purge gas washing tower C1 flows out through the methanol solution reflux outlet on the purge gas washing tower C1 and flows back to the methanol flash tank V4 through the twenty-four lines 24 connected to the methanol solution reflux outlet on the purge gas washing tower C1 and the methanol solution reflux inlet on the methanol flash tank V4.

The first methanol synthesis column R1 can be any form of methanol synthesis reactor. The tower gas enters a first methanol reactor R1, methanol synthesis reaction is carried out under the catalytic action of a copper-based catalyst, boiling water flows away from the other side, heat released by the methanol synthesis reaction is removed, meanwhile, a steam-water mixture flows out from a steam-water mixture outlet on a first methanol synthesis tower R1, the flowing steam-water mixture is sent into a first steam pocket V1 through a ninth pipeline 9 connected with a steam-water mixture outlet on a first methanol synthesis tower R1 and a first steam-water mixture inlet on a first steam pocket V1, the steam-water mixture is separated in the first steam pocket V1, medium-pressure steam for generating 2.5MPag is sent out from a medium-pressure steam outlet on the first steam pocket V1 and is sent into a steam pipe network of the whole plant through a twelfth pipeline 12 connected with the steam pipe network of the whole plant. Boiling water generated after the separation of the steam-water mixture in the first steam drum V1 flows out from a first boiling water outlet on the first steam drum V1, and is sent into the first methanol synthesis tower R1 through a tenth pipeline 10 connected with the first boiling water outlet on the first steam drum V1 and a boiling water inlet on the first methanol synthesis tower R1, so that the steam and water of the first methanol synthesis tower R1 can naturally circulate. In addition, a pump P1 may be connected in series to the tenth line 10 to forcibly circulate the boiling water in the first methanol synthesis column R1. Or according to different methanol synthesis tower forms, a pump P1 is eliminated, and the natural circulation of steam and water is adopted.

Boiler feed water at start-up of the first methanol synthesis column R1 is fed to the first drum V1 via an eleventh line 11 connected to the boiler feed water inlet on the first drum V1. In addition, the eleventh line 11 is connected to the tenth line 10 via a valve 29. A drain outlet on the first steam drum V1 is connected with a drain flash tank through a thirteenth pipeline 13.

The second methanol synthesis tower R2 can be an isothermal reactor or an adiabatic reactor according to the requirement, and the isothermal reactor is of an axial structure or a radial structure; the adiabatic reactor is of an axial structure or a radial structure.

The second methanol synthesis tower R2 is arranged at the front side of the first methanol synthesis tower R1, the tower gas enters a newly-added second methanol reactor R2, and the methanol synthesis reaction is carried out under the catalytic action of a copper-based catalyst, and a large amount of heat is released. For an isothermal reactor, boiling water is used to remove the heat evolved by the methanol synthesis reaction, while the steam-water mixture flows out through the steam-water mixture outlet on the second methanol synthesis column R2 and is fed into the second steam pocket V2 through the fourteenth line 14 connected to the steam-water mixture outlet on the second methanol synthesis column R2 and the second steam-water mixture inlet on the second steam pocket V2, and the saturated steam generated by the separation of the steam-water mixture in the second steam pocket V2 is fed out of the battery limit through the sixteenth line 16 connected to the saturated steam outlet on the second steam pocket V2.

The boiling water separated by the second steam drum V2 flows out from a second boiling water outlet on the second steam drum V2 and is sent back to the second methanol synthesis tower R2 through a fifteenth pipeline 15 connected with the second boiling water outlet on the second steam drum V2 and a steam-water mixture outlet on the second methanol synthesis tower R2, so that the steam-water natural circulation of the second methanol synthesis tower R2 is facilitated. Alternatively, depending on the actual conditions, the fourteenth line 14 and the fifteenth line 15 may be connected to the first drum V1, eliminating the second drum V2.

In addition, a second boiler feed water inlet and a second sewage draining outlet are further arranged on the second steam pocket V2, the second boiler feed water inlet is connected with boiler feed water through a thirtieth pipeline 30, and the second sewage draining outlet is connected with a sewage draining flash tank through a thirty-first pipeline 31.

Example 2

This example differs from example 1 in that: the second methanol synthesis column R2 is disposed at the rear side of the first methanol synthesis column R1 and the second drum V2 is eliminated.

The tower gas entering the tower of the embodiment is divided into two paths, one path of tower gas enters the first methanol tower R1 through the sixth pipeline 6 for reaction, the mixture of unreacted gas with the methanol concentration content of 2-10 mol% and methanol steam formed by the reaction of the first methanol tower R1 flows out of the first methanol tower R1, is mixed with the other path of tower gas through the eighteen second pipeline 28, then enters the second methanol synthesis tower R2 through the fifth pipeline 5 for reaction, the methanol solution with the methanol concentration of 16-20 mol% formed by the reaction of the second methanol tower R2 flows into the gas-gas heat exchanger E1 through the 29 pipeline 29, and the mixed gas is preheated. In addition, the mixture of unreacted gas and methanol vapor, which is formed by the reaction in the first methanol tower R1 and has a methanol concentration of 2 to 10 mol%, may be further merged into the twenty-ninth line 29 through the seventh line 7.

The utility model can be implemented for newly-built methanol synthesis projects so as to achieve the purposes of reducing investment and maximizing yield.

For projects which need energy-saving yield-increasing transformation and have other equipment with allowance, but the existing methanol synthesis tower cannot process more gas, the utility model is an effective means for solving the bottleneck of the synthesis tower.

For example, a 40 million ton methanol synthesis plant, the maximum design capacity of the plant is 110%. The device has larger allowance in the upstream and downstream working sections, but because of the defects of the original methanol synthesis tower process structure, the water side heat transfer effect is poor, the hot spot temperature of the synthesis tower is higher, the content of impurities (ethanol) in the crude methanol product is higher, and the energy consumption of the device is higher. In addition, because the structure of the ortho-methanol synthesis tower has defects, leakage is easy to occur, and the device needs to be stopped for maintenance and leakage stoppage, so that the device cannot operate under the designed load for a long time.

In order to solve the problems, the applicant connects a new methanol synthesis tower in series/parallel in front of the original methanol synthesis tower, and the newly added methanol synthesis tower adopts an isothermal tubular structure and a steam drum in consideration of the insufficient heat exchange area of the original methanol synthesis tower, and the boiler feed water takes away the reaction heat in a natural circulation mode. After the improvement of the utility model, part of fresh gas is mixed with circulating gas and then passes through the newly-added methanol reactor with the isothermal tubular structure, and because the heat exchange area of the newly-added methanol reactor with the isothermal tubular structure is large, the hot spot temperature is controllable after the methanol reaction, the impurity content in the methanol is lower, and the energy consumption of the subsequent methanol rectification can be reduced. The synthesis gas at the reaction outlet of the methanol reactor with the isothermal tubular structure is mixed with other fresh gas and then enters the original methanol synthesis tower, and because part of carbon monoxide is converted in the newly added methanol reactor with the isothermal tubular structure, the content of CO entering the original methanol synthesis tower is greatly reduced, the reaction heat is correspondingly reduced, and the problems of high hot spot temperature, poor product quality and the like of the original methanol synthesis tower caused by insufficient heat exchange area are solved.

By implementing the utility model, the net alcohol value of the system is improved by-5%, and the circulation volume of the loop is reduced by-10-30%, namely the energy consumption of the fresh air compressor and the circulating air compressor is reduced. The hot spot temperature is obviously reduced, the operation environment of the original methanol synthesis tower is mild, and the equipment leakage is not easy to occur. And because the hot spot temperature is reduced, the ethanol content in the crude methanol is reduced by about 200ppm, the product quality is obviously improved, and the unit consumption of one ton of refined methanol is also obviously reduced.

Besides adding a smaller methanol synthesis tower and a steam drum, other equipment of the loop, including a fresh gas compressor and a circulating gas compressor, do not need to be modified. The utility model improves the online rate of the device, shortens the annual parking maintenance time, prolongs the running time and better increases the economic benefit of the device.

The net value of the methanol is obviously improved after the improvement of the utility model, the circulation volume is greatly reduced, and the yield of the device can be increased in order to fully utilize the equipment capacity of the prior device. The utility model can achieve the purposes of energy saving, consumption reduction and yield increase to the maximum extent under the condition of less investment, and obviously improve the economic benefit of enterprises.

Claims (10)

1. The methanol synthesis device comprises a methanol synthesis loop, wherein the methanol synthesis loop comprises a first methanol synthesis tower, and is characterized in that a second methanol synthesis tower is additionally arranged, wherein the first methanol synthesis tower and the second methanol synthesis tower are connected in series, in series-parallel connection or in parallel connection.

2. The energy-saving or yield-increasing and consumption-reducing methanol synthesis plant according to claim 1, further comprising a fresh gas compressor, a recycle gas compressor and a gas heat exchanger, wherein the fresh gas compressor is connected to the fresh gas through a first pipeline on the one hand and a second pipeline on the other hand; the circulating gas compressor is connected with a third pipeline, the second pipeline is connected with the third pipeline and then is connected with the gas-gas heat exchanger, the gas-gas heat exchanger is connected with a fifth pipeline through a fourth pipeline, the fifth pipeline is connected with the first methanol synthesis tower or the second methanol tower is connected, the first methanol tower or the second methanol tower is connected with the second methanol synthesis tower or the first methanol synthesis tower through a sixth pipeline, the fourth pipeline is further connected with the sixth pipeline, and the first methanol tower or the second methanol tower is connected with the gas-gas heat exchanger through a seventh pipeline.

3. The energy-saving or yield-increasing and consumption-reducing methanol synthesis plant as claimed in claim 2, wherein the second methanol synthesis tower is arranged at the front side or the rear side of the first methanol synthesis tower, so as to specifically solve the practical problems of the existing plant.

4. The energy-saving or yield-increasing and consumption-reducing methanol synthesis apparatus according to claim 3, wherein the first methanol synthesis tower is any type of reactor, and the second methanol synthesis tower is an isothermal reactor or an adiabatic reactor; the isothermal reactor is of an axial structure or a radial structure; the adiabatic reactor is of an axial structure or a radial structure.

5. The energy-saving or yield-increasing and consumption-reducing methanol synthesis device according to claim 4, further comprising a first steam drum, wherein the first steam drum is provided with a first steam-water mixture inlet and a first boiled water outlet, the first steam-water mixture inlet on the first steam drum is connected with the steam-water mixture outlet on the first methanol synthesis tower through a ninth pipeline, and the first boiled water outlet on the first steam drum is connected with the boiled water inlet on the first methanol synthesis tower through a tenth pipeline, so that the steam-water natural circulation of the first methanol synthesis tower is facilitated.

6. The energy-saving or yield-increasing consumption-reducing methanol synthesis apparatus according to claim 5, wherein a pump is connected in series to the tenth line, and the pump forcibly circulates the boiling water in the first methanol synthesis tower.

7. The energy-saving or yield-increasing and consumption-reducing methanol synthesis device according to claim 6, wherein the first steam drum is further provided with a first boiler feed water inlet, an intermediate pressure steam outlet and a first blowdown port, the first boiler feed water inlet is connected with boiler feed water through an eleventh pipeline, and the intermediate pressure steam outlet is connected with a steam pipe network through a twelfth pipeline; the first sewage discharge port is connected with a sewage discharge flash tank through a thirteenth pipeline; the eleventh pipeline and the tenth pipeline are connected through a valve.

8. The energy-saving or yield-increasing and consumption-reducing methanol synthesis device according to claim 7, further comprising a second steam drum, wherein the second steam drum is provided with a second steam-water mixture inlet and a second boiling water outlet, the second steam-water mixture inlet on the second steam drum is connected with the steam-water mixture outlet on the second methanol synthesis tower through a fourteenth pipeline, and the second boiling water outlet on the second steam drum is connected with the boiling water inlet on the second methanol synthesis tower through a fifteenth pipeline, so that the steam-water natural circulation of the second methanol synthesis tower is facilitated; or the fourteenth pipeline and the fifteenth pipeline are connected with the first steam drum according to the actual working condition, and the second steam drum is eliminated.

9. The energy-saving or yield-increasing and consumption-reducing methanol synthesis device as claimed in claim 8, wherein the second steam drum is further provided with a saturated steam outlet, a second boiler feed water inlet and a second sewage outlet, and the saturated steam from the saturated steam outlet is sent out of the battery limit through a sixteenth pipeline; the second boiler feed water inlet is connected with boiler feed water through a thirtieth pipeline, and the second sewage discharge outlet is connected with a sewage discharge flash tank through a thirty-first pipeline.

10. The energy-saving or yield-increasing and consumption-reducing methanol synthesis device according to any one of claims 2 to 9, further comprising a high-pressure methanol separator, a methanol flash tank and a purge gas washing tower, wherein the high-pressure methanol separator is provided with a methanol solution inlet, a separated gas outlet and a separated liquid outlet; a separated liquid inlet, a crude methanol outlet, a fuel gas outlet and a methanol solution backflow inlet are arranged on the methanol flash tank; the purge gas washing tower is provided with a washing water inlet, a separation gas inlet, a purge gas outlet and a methanol solution reflux outlet; a methanol solution inlet on the high-pressure methanol separator is connected with a methanol solution outlet on the gas-gas heat exchanger through a seventeenth pipeline and a water cooler, a separated gas outlet on the high-pressure methanol separator is connected with an inlet of a circulating gas compressor through an eighteenth pipeline on one hand, and is connected with a separated gas inlet on the purge gas washing tower through a nineteenth pipeline on the other hand, and the nineteenth pipeline is also connected with a torch through a twentieth pipeline; a separated liquid outlet on the high-pressure methanol separator is connected with a separated liquid inlet on the methanol flash tank through a twenty-one pipeline; the coarse methanol outlet on the methanol flash tank is connected with a downstream methanol rectification unit or an intermediate tank through a twenty-two pipeline, the fuel gas outlet on the methanol flash tank is connected with a torch through a twenty-three pipeline, the methanol solution reflux inlet on the methanol flash tank is connected with the methanol solution reflux outlet on the purge gas washing tower through a twenty-four pipeline, the washing water inlet on the purge gas washing tower is connected with washing water through a twenty-five pipeline, and the purge gas outlet on the purge gas washing tower is sent out of a boundary area through a twenty-six pipeline.

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