CN218793953U - Refining device for preparing methanol product by carbon dioxide hydrogenation - Google Patents
Refining device for preparing methanol product by carbon dioxide hydrogenation Download PDFInfo
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Abstract
The utility model belongs to the technical field of methyl alcohol rectification, a carbon dioxide hydrogenation system methyl alcohol product refining plant is related to. The device comprises a pre-rectifying tower, a pressurizing tower and an atmospheric tower. The pressurizing tower top outlet pipeline is connected with the pressurizing tower reflux tank through a normal pressure tower reboiler, the bottom outlet liquid phase pipeline is connected with the normal pressure tower through a pre-tower reboiler, and the bottom outlet liquid phase pipeline of the normal pressure tower is conveyed to the outside through a normal pressure tower bottom waste water pump and a pre-tower feeding preheater. The utility model discloses with the top of the tower ejection of compact heat of pressurized column as the reboiler heat source of atmospheric tower, tower cauldron ejection of compact heat is as the reboiler heat source of pre-rectification tower, and the rectifying that is used for preheating pre-rectification tower is handled to the tower cauldron of atmospheric tower, has advantages such as energy integration is effectual, can obtain good operational benefits.
Description
Technical Field
The utility model belongs to the technical field of methyl alcohol rectification, a carbon dioxide hydrogenation system methyl alcohol product refining plant is related to.
Background
Methanol is an important basic chemical raw material and can also be used as fuel. Methanol synthesis and rectification are two steps in the preparation of a refined methanol product. The traditional process for synthesizing methanol mainly comprises carbon monoxide (CO) and hydrogen (H) 2 ) The methanol is obtained as a raw material under the action of a catalyst, and the correspondingly matched methanol rectification usually adopts a five-tower rectification technology and can be divided into a pre-tower, a vacuum tower, a pressurizing tower, an atmospheric tower and a recovery tower according to different pressures.
Patent CN110280034A reports a system comprising a light component removal tower, a vacuum rectification tower, a pressure rectification tower, an atmospheric rectification tower and a recovery tower, which is further optimized compared with the traditional five-tower process. The pre-tower is still heated by externally supplied steam, the heat source of the pressure reducing tower is from low-level heat of methanol synthesis gas, and the pressurizing tower, the atmospheric tower, the pressure reducing tower and the light tower are multiple-effect, so that the effect of saving steam is achieved.
Patent CN111116317A discloses a five-tower four-effect methanol rectification process and equipment, which mainly comprise a pre-rectification tower, a first pressurizing tower, a second pressurizing tower, a third pressurizing tower, a steam reduced pressure flash tank, a kettle liquid buffer tank, a recovery tower and the like, and the problems of kettle liquid level fluctuation of the three rectification towers and feed fluctuation of the recovery tower are solved by adding the kettle liquid buffer tank, so that the operation difficulty of the recovery tower is reduced.
However, the rectification process is directed to a process for preparing methanol by hydrogenating carbon monoxide, wherein H in crude methanol 2 Under the condition of low O content, the temperature gradient between the top and the bottom of the tower is small, only a small pressure difference is needed among the towers, the temperature difference between the methanol steam at the top of the tower at the upper stage and the methanol at the bottom of the tower at the lower stage can be formed, carbon dioxide is used as a raw material for preparing the methanol, the molar ratio of the methanol to byproduct water is 1:1, the high water content of crude methanol increases the temperature difference between the top of the tower and the bottom of the tower, the problem of temperature difference increase is more prominent along with the separation of the methanol, if the rectification process is still adopted, the pressure difference among the towers at all stages has to be increased in order to ensure the temperature difference between the steam at the top of the tower at the upper stage and the bottom of the tower at the lower stage, the equipment investment is obviously increased, and the steam grade and the consumption of a reboiler of the high-pressure tower are also increased; in addition, the traditional process has no effective energy integration optimization, which results in high steam consumption and high production and operation cost.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to the weak point that prior art exists, and a carbon dioxide hydrogenation system methyl alcohol product refining technology and device is provided, the process flow design has adopted 3+1 technology, 3 rectifying column (pre-rectifying tower, pressurized column and atmospheric tower) and 1 tail gas scrubbing tower promptly, the top of the tower ejection of compact heat as the reboiler heat source of atmospheric tower with the pressurized column, tower cauldron ejection of compact heat is as the reboiler heat source of pre-rectifying tower, the rectifying that is used for preheating pre-rectifying tower is handled to the tower cauldron of atmospheric tower, have advantages such as energy integration is effectual.
The purpose of the utility model can be realized by the following technical scheme:
a refining device for preparing a methanol product by carbon dioxide hydrogenation comprises a pre-rectifying tower, a pressurizing tower and an atmospheric tower;
a crude methanol output pipeline from the outside is sequentially connected with a pre-rectifying tower feed pump, a pre-rectifying tower feed preheater and a pre-rectifying tower, an outlet pipeline at the top of the pre-rectifying tower is sequentially connected with the pre-rectifying tower through a pressurizing tower reflux pump and a pre-rectifying tower reflux tank, and a gas phase outlet pipeline of the pre-rectifying tower reflux tank is connected with a pre-rectifying tower tail gas washing tower; the outlet pipeline at the bottom of the pre-rectifying tower is connected with the pressurizing tower through a pressurizing tower feed pump;
the outlet pipeline at the top of the pressurizing tower is connected with a reflux tank of the pressurizing tower through an atmospheric tower reboiler, and the outlet liquid phase pipeline at the bottom of the pressurizing tower is connected with the atmospheric tower through a pre-tower reboiler;
the atmospheric tower top outlet pipeline is connected with the atmospheric tower reflux tank through an atmospheric tower cooler, and the atmospheric tower bottom outlet liquid phase pipeline is sequentially conveyed to the outside after passing through an atmospheric tower bottom waste water pump and a pre-tower feeding preheater.
The utility model discloses among the technical scheme: an outlet liquid phase pipeline at the bottom of the reflux tank of the pressurizing tower is divided into two parts, wherein one part is sent to the crude methanol tank, and the other part returns to the pressurizing tower through a reflux pump of the pressurizing tower.
The utility model discloses among the technical scheme: the liquid phase pipeline at the outlet of the reflux tank of the atmospheric tower is divided into two streams, wherein one stream is sent to the crude methanol tank, and the other stream is connected with the atmospheric tower through a reflux pump of the atmospheric tower.
A method for refining a methanol product prepared by carbon dioxide hydrogenation by using the device comprises the following steps:
1) Crude methanol from the outside is heated by a pre-tower feeding preheater and then enters a pre-rectifying tower, a gas phase at the top of the pre-rectifying tower is cooled by a pre-tower cooler and then enters a pre-tower reflux tank, a liquid phase material in the pre-tower reflux tank returns to the pre-rectifying tower, and the gas phase enters a pre-tower tail gas washing tower; liquid phase at an outlet at the bottom of the pre-rectifying tower is conveyed to a pressurizing tower;
2) Cooling a gas phase at an outlet at the top of the pressurizing tower through a reboiler of the normal pressure tower, and then feeding the gas phase into a reflux tank of the pressurizing tower, wherein non-condensable gas at the top of the reflux tank of the pressurizing tower returns to an outlet pipeline at the top of the pressurizing tower; cooling the liquid phase at the outlet of the bottom of the pressurizing tower by a pre-tower reboiler and then feeding the liquid phase into the normal pressure tower;
3) And the gas phase at the outlet of the top of the atmospheric tower is cooled by an atmospheric tower cooler and then enters an atmospheric tower reflux tank, and the liquid phase at the outlet of the bottom of the atmospheric tower is sent to the outside after passing through an atmospheric tower bottom waste water pump and a pre-tower feeding preheater.
The method comprises the following steps: the operation temperature of the pre-rectifying tower is controlled to be 90-150 ℃, and the operation pressure is controlled to be 0.2-0.4 MPag.
The method comprises the following steps: the operation temperature of the pressurizing tower is controlled to be 120-150 ℃, and the operation pressure is controlled to be 0.6-0.9 MPag.
The method comprises the following steps: the operating temperature of the atmospheric tower is controlled to be 60-110 ℃, and the operating pressure is controlled to be 0.02-0.06 MPag.
The utility model has the advantages that:
the process and the device for refining the methanol product prepared by carbon dioxide hydrogenation use the top discharge heat of a pressurizing tower as a reboiler heat source of an atmospheric tower, use the bottom discharge heat as a reboiler heat source of a pre-rectifying tower, and use the bottom treatment of the atmospheric tower for preheating the rectification of the pre-rectifying tower.
Drawings
Fig. 1 is a schematic view of the process of the present invention.
In the figure: 1-a pre-tower feed pump, 2-a pre-tower feed preheater, 3-a pre-rectifying tower, 4-a pressurizing tower reflux pump, 5-a pre-tower reflux tank, 6-a pre-tower reflux pump, 7-a pre-tower tail gas washing tower, 8-a pre-tower reboiler, 9-a pressurizing tower feed pump, 10-a pressurizing tower, 11-a pressurizing tower reboiler, 12-an atmospheric tower reboiler, 13-a pressurizing tower reflux tank, 14-a crude methanol tank, 15-an atmospheric tower, 16-an atmospheric tower bottom waste water pump, 17-an atmospheric tower cooler, 18-an atmospheric tower reflux tank and 19-an atmospheric tower reflux pump.
Detailed Description
The present invention will be further explained with reference to the following embodiments, but the scope of the present invention is not limited thereto:
referring to fig. 1, a refining apparatus for producing methanol by hydrogenation of carbon dioxide comprises a pre-rectifying tower 3, a pressurized tower 10 and an atmospheric tower 15; a crude methanol output pipeline from the outside is sequentially connected with a pre-rectifying tower feed pump 1, a pre-rectifying tower feed preheater 2 and a pre-rectifying tower 3, and an outlet pipeline at the top of the pre-rectifying tower 3 is connected with a pre-rectifying tower reflux tank 5 through a pressurizing tower reflux pump 4; a liquid phase outlet pipeline of the pre-tower reflux tank 5 is connected with the pre-rectifying tower 3 through a pre-tower reflux pump 6, and a gas phase outlet pipeline of the pre-tower reflux tank 5 is connected with a pre-tower tail gas washing tower 7; the upper part of the pre-tower tail gas washing tower 7 is provided with a desalted water input pipeline, and the bottom of the pre-tower tail gas washing tower is provided with a waste liquid discharge pipeline. The outlet pipeline at the bottom of the pre-rectifying tower 3 is connected with a pressurizing tower 10 through a pressurizing tower feeding pump 9.
An outlet pipeline at the top of the pressurizing tower 10 is connected with a pressurizing tower reflux tank 13 through an atmospheric tower reboiler 12, non-condensable gas at the top of the pressurizing tower reflux tank 13 returns to the outlet pipeline at the top of the pressurizing tower 10, an outlet liquid phase pipeline at the bottom of the pressurizing tower reflux tank 13 is divided into two parts, one part is sent to a crude methanol tank 14, and the other part returns to the pressurizing tower 10 through a pressurizing tower reflux pump 4; the outlet liquid phase pipeline at the bottom of the pressurizing tower 10 is connected with the atmospheric tower 15 through a pre-tower reboiler 8;
an outlet pipeline at the top of the atmospheric tower 15 is connected with an atmospheric tower reflux tank 18 through an atmospheric tower cooler 17, an outlet liquid phase pipeline of the atmospheric tower reflux tank 18 is divided into two parts, one part is sent to a crude methanol tank 14, and the other part returns to the atmospheric tower 15 through an atmospheric tower reflux pump 19; and the liquid phase pipeline at the outlet of the bottom of the atmospheric tower 10 is sent to the outside through a waste water pump 16 at the bottom of the atmospheric tower and a pre-tower feeding preheater 2.
Example 1
Crude methanol with the out-of-range flow of 23840kg/h and the temperature of 40 ℃ is boosted by a pre-tower feeding pump, heated to 68 ℃ by a pre-tower feeding preheater and then enters a pre-rectifying tower, the operation temperature is controlled to be 90-120 ℃, and the operation pressure is controlled to be 0.2MPag. The gas phase flow at the top of the pre-rectifying tower is 3358kg/h, the temperature is 90 ℃, and the gas phase enters a pre-rectifying tower reflux tank after being cooled to 40 ℃ by a pressurizing tower reflux pump. 1787kg/h of liquid-phase material in the pre-tower reflux tank is pressurized by a pre-tower reflux pump and then returns to the pre-rectifying tower, and the gas-phase flow is 806Nm 3 The effluent gas enters a pre-tower tail gas washing tower and is in countercurrent contact with desalted water with the flow rate of 1000kg/h from the outside, and the flow rate of the non-condensable gas is 672Nm 3 The effluent was purged at the top and sent out at a bottom flow rate of 1360 kg/h. And (3) boosting the liquid phase at the outlet of the bottom of the pre-rectifying tower by a charging pump of a pressurizing tower, and then feeding the liquid phase into the pressurizing tower, wherein the operating temperature is controlled to be 120-145 ℃, and the operating pressure is controlled to be 0.6MPag. The gas phase flow at the outlet of the top of the pressurizing tower is 2845Nm 3 /h，The non-condensable gas at the top of the pressurizing tower reflux tank returns to an outlet pipeline at the top of the pressurizing tower after being cooled to 40 ℃ by an atmospheric tower reboiler, the flow of the liquid phase at the outlet at the bottom of the pressurizing tower reflux tank is 3890kg/h and is divided into two parts, wherein one part is sent to a crude methanol tank at the flow of 2334kg/h, and the other part is returned to the pressurizing tower through a pressurizing tower reflux pump at the flow of 1556 kg/h; 19931kg/h of liquid phase at the bottom outlet of the pressurizing tower is cooled by a pre-tower reboiler at 52 ℃ and then enters the normal pressure tower, the operation temperature is controlled at 60-90 ℃, and the operation pressure is controlled at 0.02MPag. The flow rate of the gas phase at the outlet of the top of the atmospheric tower is 7616Nm 3 Cooling to 40 ℃ by using a cooler of the normal pressure tower, then feeding the cooled liquid into a reflux tank of the normal pressure tower, dividing the liquid phase flow at the outlet of the reflux tank of the normal pressure tower into two flows, wherein one flow is 8011kg/h, sending the liquid phase flow to a crude methanol tank, and the other flow is 2883kg/h, and returning the liquid phase flow to the normal pressure tower through a reflux pump of the normal pressure tower; the liquid phase flow at the bottom outlet of the atmospheric tower is 11920kg/h, and the liquid phase is cooled to 40 ℃ by an atmospheric tower bottom waste water pump and a pre-tower feeding preheater and then sent out.
Example 2
Crude methanol with the out-of-range flow of 23840kg/h and the temperature of 40 ℃ is boosted by a pre-tower feeding pump, heated to 111 ℃ by a pre-tower feeding preheater and then enters a pre-rectifying tower, the operation temperature is controlled to be 114-142 ℃, and the operation pressure is controlled to be 0.3MPag. The gas phase flow at the top of the pre-rectifying tower is 3346kg/h, the temperature is 90 ℃, and the gas phase enters a pre-rectifying tower reflux tank after being cooled to 40 ℃ by a pressurizing tower reflux pump. Liquid phase material 2491kg/h in the pre-tower reflux tank is pressurized by a pre-tower reflux pump and then returns to the pre-rectifying tower, and the gas phase flow is 806Nm 3 The effluent gas enters a pre-tower tail gas washing tower and is in countercurrent contact with desalted water with the flow rate of 1000kg/h from the outside, and the flow rate of the non-condensable gas is 291Nm 3 The waste liquid is discharged from the top after being purified, and the bottom flow is 1587kg/h and is sent to the outside. And (3) boosting the liquid phase at the outlet of the bottom of the pre-rectifying tower by a charging pump of a pressurizing tower, and then feeding the liquid phase into the pressurizing tower, wherein the operating temperature is controlled to be 130-145 ℃, and the operating pressure is controlled to be 0.75MPag. The gas phase flow at the outlet of the top of the pressurizing tower is 2845Nm 3 Cooling to 40 deg.C by a reboiler of the atmospheric tower, feeding into a reflux tank of the pressurizing tower, returning the non-condensable gas at the top of the reflux tank of the pressurizing tower to an outlet pipeline at the top of the pressurizing tower, and refluxing in the pressurizing towerThe liquid phase flow at the outlet of the bottom of the tank is 4046kg/h and is divided into two flows, wherein one flow is 2440kg/h and is sent to a crude methanol tank, and the other flow is 1627kg/h and returns to a pressurizing tower through a pressurizing tower reflux pump; the liquid phase at the bottom outlet 20541kg/h of the pressurizing tower is cooled to 59 ℃ by a pre-tower reboiler and then enters the normal pressure tower, the operation temperature is controlled to be 55-98 ℃, and the operation pressure is controlled to be 0.03MPag. The gas phase flow at the outlet of the top of the atmospheric tower is 13216Nm 3 Cooling to 40 ℃ by using an atmospheric tower cooler, then feeding into an atmospheric tower reflux tank, dividing a liquid phase flow at an outlet of the atmospheric tower reflux tank into two flows, wherein one flow is 8087kg/h, sending the two flows to a crude methanol tank, and the other flow is 10997kg/h, and returning to the atmospheric tower through an atmospheric tower reflux pump; the liquid phase flow at the bottom outlet of the atmospheric tower is 12455kg/h, and the liquid phase is cooled to 40 ℃ by an atmospheric tower bottom waste water pump and a pre-tower feeding preheater and then is sent out.
Example 3
Crude methanol with the out-of-range flow of 23840kg/h and the temperature of 40 ℃ is boosted by a pre-tower feeding pump, heated to 114 ℃ by a pre-tower feeding preheater and then enters a pre-rectifying tower, the operation temperature is controlled to be 120-150 ℃, and the operation pressure is controlled to be 0.4MPag. The gas phase flow at the top of the pre-rectifying tower is 3402kg/h, the temperature is 90 ℃, and the gas phase enters a pre-rectifying tower reflux tank after being cooled to 40 ℃ by a pressurizing tower reflux pump. Liquid phase material 2706kg/h of the pre-tower reflux tank is pressurized by a pre-tower reflux pump and then returns to the pre-rectifying tower, and the gas phase flow is 358Nm 3 The effluent gas enters a pre-tower tail gas washing tower and is in countercurrent contact with desalted water with the flow rate of 1800kg/h from the outside, and the flow rate of the non-condensable gas is 157Nm 3 The waste liquid is discharged from the top after being purified, and the bottom flow is 2219 kg/h. And (3) boosting the liquid phase at the outlet of the bottom of the pre-rectifying tower by a charging pump of a pressurizing tower, and then feeding the liquid phase into the pressurizing tower, wherein the operating temperature is controlled to be 136-150 ℃, and the operating pressure is controlled to be 0.75MPag. The gas phase flow at the outlet of the top of the pressurizing tower is 2845Nm 3 Cooling to 40 ℃ by a reboiler of the atmospheric tower, feeding the cooled gas into a reflux tank of the pressurizing tower, returning the non-condensable gas at the top of the reflux tank of the pressurizing tower to an outlet pipeline at the top of the pressurizing tower, dividing the liquid phase flow at the bottom of the reflux tank of the pressurizing tower into two parts, wherein one part is fed into a crude methanol tank at 2443kg/h, and the other part is fed into a reflux pump of the pressurizing tower at 1629kg/hReturning to the pressurizing tower; 20698kg/h of liquid phase at the bottom of the pressurizing tower is cooled to 67 ℃ by a pre-tower reboiler and then enters the normal pressure tower, the operation temperature is controlled to be 59-105 ℃, and the operation pressure is controlled to be 0.06MPag. The gas phase flow at the outlet of the top of the atmospheric tower is 13216Nm 3 Cooling to 40 ℃ by using a normal pressure tower cooler, and then feeding the cooled product into a normal pressure tower reflux tank, wherein the liquid phase flow at the outlet of the normal pressure tower reflux tank is 19167kg/h and is divided into two streams, one stream is 8122kg/h and is sent to a crude methanol tank, and the other stream is 11045kg/h and is returned to the normal pressure tower through a normal pressure tower reflux pump; the liquid phase flow at the bottom outlet of the atmospheric tower is 12576kg/h, and the liquid phase is cooled to 40 ℃ by an atmospheric tower bottom waste water pump and a pre-tower feeding preheater and then is sent out.
In the above example, the steam consumption of the rectifier reboiler was compared to the conventional process, as shown in table 1:
TABLE 1 steam consumption COMPARATIVE TABLE (kg/h)
As can be seen from the table 1, compared with the traditional process, the process of the utility model has better energy integration effect, the steam consumption reduction percentage is about 33% -38%, and the process has good operation benefit. The foregoing embodiments and description only illustrate the principles of the present invention and do not limit the scope of the invention, and the present invention will be further modified without departing from the spirit and scope of the invention, which falls within the scope of the invention as claimed. The utility model discloses the part that does not relate to all is the same with prior art or can adopt prior art to realize.
Claims (3)
1. A carbon dioxide hydrogenation system methyl alcohol product refining plant which characterized in that: the device comprises a pre-rectifying tower (3), a pressurizing tower (10) and an atmospheric tower (15);
a crude methanol output pipeline from the outside is sequentially connected with a pre-rectifying tower feed pump (1), a pre-rectifying tower feed preheater (2) and a pre-rectifying tower (3), an outlet pipeline at the top of the pre-rectifying tower (3) is sequentially connected with the pre-rectifying tower (3) through a pressurizing tower reflux pump (4) and a pre-rectifying tower reflux tank (5), and a gas phase outlet pipeline of the pre-rectifying tower reflux tank (5) is connected with a pre-rectifying tower tail gas washing tower (7); an outlet pipeline at the bottom of the pre-rectifying tower (3) is connected with a pressurizing tower (10) through a pressurizing tower feed pump (9);
an outlet pipeline at the top of the pressurized tower (10) is connected with a reflux tank (13) of the pressurized tower through an atmospheric tower reboiler (12), and an outlet liquid phase pipeline at the bottom of the pressurized tower (10) is connected with an atmospheric tower (15) through a pre-tower reboiler (8);
the top outlet pipeline of the atmospheric tower (15) is connected with an atmospheric tower reflux tank (18) through an atmospheric tower cooler (17), and a bottom outlet liquid phase pipeline of the atmospheric tower (15) is sequentially sent to the outside after passing through an atmospheric tower bottom waste water pump (16) and a pre-tower feeding preheater (2).
2. The refining device for methanol products by carbon dioxide hydrogenation according to claim 1, characterized in that: the outlet liquid phase pipeline at the bottom of the pressurizing tower reflux tank (13) is divided into two parts, wherein one part is sent to a crude methanol tank (14), and the other part returns to the pressurizing tower (10) through a pressurizing tower reflux pump (4).
3. The refining device for methanol products by carbon dioxide hydrogenation according to claim 1, characterized in that: the liquid phase pipeline at the outlet of the reflux tank (18) of the atmospheric tower is divided into two parts, wherein one part is sent to the crude methanol tank (14), and the other part is connected with the atmospheric tower (15) through a reflux pump (19) of the atmospheric tower.
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