CN210346070U

CN210346070U - Methanol-to-olefin heat exchange system

Info

Publication number: CN210346070U
Application number: CN201921038999.3U
Authority: CN
Inventors: 吕名; 张栋
Original assignee: Lianhong New Materials Technology Co Ltd
Current assignee: Lianhong New Materials Technology Co Ltd
Priority date: 2019-07-05
Filing date: 2019-07-05
Publication date: 2020-04-17
Anticipated expiration: 2029-07-05

Abstract

The utility model relates to a methanol-to-olefin heat exchange system belongs to coal chemical industry equipment technical field, including the rectifying column, the top of the tower of rectifying column is connected with the condenser, and the tower bottom of rectifying column is connected with reboiler, the surface and/or the internal surface of the heat exchange tube of condenser and/or reboiler are provided with the metal porous layer, the condenser is connected with the backward flow jar, and the backward flow jar passes through the backflow pipeline to be connected with the rectifying column, install the backwash pump on the backflow pipeline. The utility model has the advantages of multiplicable heat load and heat transfer volume can satisfy the requirement that equipment productivity increases.

Description

Methanol-to-olefin heat exchange system

Technical Field

The utility model relates to a methanol-to-olefin heat transfer system belongs to coal chemical industry equipment technical field.

Background

The olefin is a basic raw material of petrochemical industry, the downstream product is a polyolefin plastic product, the application is very wide, the technology for preparing the olefin from the methanol can overcome the problem of the dependence on petroleum resources on the production of the olefin, and the production cost can be reduced. A complete methanol to olefins plant typically has an annual olefin product production rate designed, however, with increasing market demand, to improve production economics, increased capacity is required, but a simple yearly replacement of a more productive plant requires a large cost investment, thus technically retrofitting an existing methanol to olefins plant. In design accounting and actual operation, the heat exchange system of the equipment in the improvement can not meet the requirement after the increase, so that the problem that how to enable the heat exchange system to meet the requirement after the increase in production of the equipment is required to be solved is found.

Disclosure of Invention

For solving above technological not enough, the utility model provides a methanol to olefin heat transfer system, multiplicable heat load and heat transfer volume can satisfy the requirement that equipment productivity increases.

The technical scheme of the utility model as follows: the utility model provides a methanol-to-olefin heat transfer system, includes the rectifying column, the top of the tower of rectifying column is connected with the condenser, and the tower bottom of rectifying column is connected with the reboiler, the surface and/or the internal surface of the heat exchange tube of condenser and/or reboiler are provided with the metal porous layer, the condenser is connected with the reflux tank, and the reflux tank passes through the backflow pipeline and is connected with the rectifying column, install the backwash pump on the backflow pipeline.

The technical scheme of the utility model still include: the rectifying tower comprises a deethanizer, the top of the deethanizer is connected with a deethanizer condenser used for condensing a gas phase part at the top of the deethanizer into a liquid phase, the bottom of the deethanizer is connected with a deethanizer reboiler used for gasifying a liquid phase part at the bottom of the deethanizer, and heat exchange tubes of the deethanizer condenser and the deethanizer reboiler are provided with metal porous layers on the outer surface and/or the inner surface.

The technical scheme of the utility model still include: the rectifying tower comprises an ethylene rectifying tower, the top of the ethylene rectifying tower is connected with an ethylene rectifying tower condenser used for condensing a gas phase part on the top of the tower into a liquid phase, the bottom of the ethylene rectifying tower is connected with an ethylene rectifying tower reboiler used for gasifying a liquid phase part in a tower bottom, and heat exchange tubes of the ethylene rectifying tower condenser and the ethylene rectifying tower reboiler are provided with metal porous layers on the outer surface and/or the inner surface.

The technical scheme of the utility model still include: the rectifying tower comprises a high-pressure depropanizing tower, the top of the high-pressure depropanizing tower is connected with a high-pressure depropanizing tower condenser used for condensing a gas phase part at the top of the tower into a liquid phase, the bottom of the high-pressure depropanizing tower is connected with a high-pressure depropanizing tower reboiler used for gasifying a liquid phase part at the bottom of the tower, and the outer surface and/or the inner surface of a heat exchange tube of the high-pressure depropanizing tower condenser is/are provided with a metal porous layer.

The technical scheme of the utility model still include: the rectifying tower comprises a propylene rectifying tower, the top of the propylene rectifying tower is connected with a propylene rectifying tower condenser used for condensing a gas phase part on the top of the tower into a liquid phase, the bottom of the propylene rectifying tower is connected with a propylene rectifying tower reboiler used for gasifying a liquid phase part in a tower kettle, and a metal porous layer is arranged on the outer surface and/or the inner surface of a heat exchange tube of the propylene rectifying tower condenser.

The technical scheme of the utility model still include: the heat exchange tube of the propylene refrigerant condenser is characterized by further comprising a propylene refrigerant condenser, wherein the propylene refrigerant condenser is connected with a propylene machine and used for condensing gas-phase propylene at the outlet of the propylene machine into liquid-phase propylene, and a metal porous layer is arranged on the outer surface and/or the inner surface of the heat exchange tube of the propylene refrigerant condenser.

The utility model has the advantages that: the metal porous layers are arranged on the outer surface and the inner surface of the heat exchange tubes of the condenser and the reboiler which have the heat transfer function, so that the high-efficiency heat transfer under the low temperature difference is realized, the boiling heat transfer can be enhanced, the cascade utilization of energy sources is favorably realized, the energy utilization rate can be improved, the waste heat emission is reduced, and the heat exchanger has the following advantages:

1) the condenser and the reboiler with the metal porous layer have high heat transfer coefficient. The boiling is always kept in a nucleate boiling state, and the boiling heat supply coefficient is 3-8 times that of a common light tube, so that the total heat transfer coefficient of the boiling equipment is greatly improved.

2) The cost performance is high. Because the heat transfer efficiency is improved, the equipment volume is reduced, the equipment investment is reduced, the corresponding construction cost is reduced, and the higher cost performance is embodied.

Drawings

Fig. 1 is a schematic diagram of the present invention.

1. The system comprises a condenser, 2, a reboiler, 3, a rectifying tower, 4, a reflux tank, 5 and a reflux pump.

Detailed Description

The present invention will be further explained by way of examples with reference to the accompanying drawings.

As shown in fig. 1, the utility model discloses a methanol-to-olefin heat transfer system mainly carries out the heat transfer optimization to the rectifying column 3 of equipment, generally, can be connected with condenser 1 at the top of the tower of rectifying column 3 to the gas phase part of following the top of the tower combustion gas condenses into the liquid phase, later the liquid phase product gets into reflux tank 4, in reentrant rectifying column 3 under the effect of backwash pump 5. Meanwhile, a reboiler 2 is connected to the bottom of the rectifying column 3, and the liquid phase discharged from the column bottom is vaporized by the reboiler 2.

The utility model discloses in, for increase heat load and heat transfer volume to the operation bottleneck of elimination equipment improves the productivity, sets up the metal porous layer on the heat exchange tube surface of the condenser 1 of being connected with 3 tops of the tower of rectifying column, sets up the metal porous layer on the heat exchange tube surface of the reboiler 2 of being connected at the bottom of 3 towers with the rectifying column.

The embodiment of the utility model provides an in, can select only to set up the metal porous layer on condenser 1 or reboiler 2's heat exchange tube surface according to the heat load of equipment and heat transfer volume needs, also can set up the metal porous layer on condenser 1 and reboiler 2's surface simultaneously. In addition, the metal porous layer can be arranged on the inner surface or the outer surface of the heat exchange tube only, or can be arranged on both the inner surface and the outer surface.

The embodiment of the utility model provides an in, rectifying column 3 is including the deethanizer, and the component in the product gas can separate in the deethanizer, and wherein, the top of the tower is carbon two and above component, and the tower cauldron is carbon three and following component. The top of the deethanizer is connected with a deethanizer condenser used for condensing a gas phase part at the top of the deethanizer into a liquid phase, the bottom of the deethanizer is connected with a deethanizer reboiler used for gasifying a liquid phase part at the bottom of the deethanizer, and the surfaces of heat exchange tubes of the deethanizer condenser and the deethanizer reboiler are respectively provided with a metal porous layer.

In another embodiment of the present invention, the rectifying tower 3 comprises an ethylene rectifying tower for separating the carbon dioxide component in the feed, wherein the tower bottom is the ethane component, and the ethylene product is extracted from the eighth layer of the tower plate. The top of the ethylene rectifying tower is connected with an ethylene rectifying tower condenser for condensing a gas phase part on the top of the tower into a liquid phase, the bottom of the ethylene rectifying tower is connected with an ethylene rectifying tower reboiler for gasifying a liquid phase part in a tower kettle, and the surfaces of heat exchange tubes of the ethylene rectifying tower condenser and the ethylene rectifying tower reboiler are respectively provided with a metal porous layer.

In another embodiment of the present invention, the distillation column 3 comprises a high pressure depropanizer for separating the carbon three and the following components in the feed, wherein the top of the column is carbon three and the bottom of the column is carbon four or less. The top of the high-pressure depropanizing tower is connected with a high-pressure depropanizing tower condenser used for condensing the gas phase part at the top of the tower into a liquid phase, the bottom of the high-pressure depropanizing tower is connected with a high-pressure depropanizing tower reboiler used for gasifying the liquid phase part at the bottom of the tower, and the surface of a heat exchange tube of the high-pressure depropanizing tower condenser is only provided with a metal porous layer.

In another embodiment of the present invention, the distillation column 3 comprises a propylene distillation column for separating propylene and propane in the feed, wherein the top of the column is propylene product and the bottom of the column is propane product. The top of the propylene rectifying tower is connected with a propylene rectifying tower condenser used for condensing a gas phase part at the top of the tower into a liquid phase, the bottom of the propylene rectifying tower is connected with a propylene rectifying tower reboiler used for gasifying a liquid phase part at the bottom of the tower, and a metal porous layer is arranged on the surface of a heat exchange tube of the propylene rectifying tower condenser.

The utility model discloses a further embodiment, heat transfer system still includes propylene refrigerant condenser, and this propylene refrigerant condenser uses the circulating water to become liquid phase propylene with the gaseous phase propylene condensation of propylene machine export, improves liquid phase propylene refrigerant for the device. Similarly, the surface of the heat exchange tube of the propylene refrigerant condenser is also provided with a metal porous layer to improve the heat transfer effect and meet the requirement of increasing the yield.

Adopt the utility model discloses a behind the heat transfer system, former design methyl alcohol feed volume is 125 tons/hour (book pure), handles 100 ten thousand tons/year methyl alcohol (book pure) annually promptly, produces the equipment of 33 ten thousand tons/year alkene (ethylene + propylene) products (alkene output uses the gas volume of gas compressor entry as the benchmark), increases to 43 ten thousand tons/year alkene (ethylene + propylene) at the productivity of reforming transform back device.

The above description is only a preferred embodiment of the present invention, and is not intended to limit the present invention in any way, and any modification, equivalent replacement, and improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. The utility model provides a methanol-to-olefin heat transfer system, includes rectifying column (3), its characterized in that: the top of rectifying column (3) is connected with condenser (1), and the bottom of rectifying column (3) is connected with reboiler (2), the surface and/or the internal surface of the heat exchange tube of condenser (1) and/or reboiler (2) are provided with the metal porous layer, condenser (1) is connected with reflux tank (4), and reflux tank (4) are connected with rectifying column (3) through the backflow pipeline, install backwash pump (5) on the backflow pipeline.

2. The methanol-to-olefin heat exchange system of claim 1, wherein: the rectifying tower (3) comprises a deethanizer, the top of the deethanizer is connected with a deethanizer condenser used for condensing a gas phase part at the top of the tower into a liquid phase, the bottom of the deethanizer is connected with a deethanizer reboiler used for gasifying a liquid phase part at the bottom of the tower, and heat exchange tubes of the deethanizer condenser and the deethanizer reboiler are provided with metal porous layers on the outer surface and/or the inner surface.

3. The methanol-to-olefin heat exchange system of claim 1, wherein: the rectifying tower (3) comprises an ethylene rectifying tower, wherein the top of the ethylene rectifying tower is connected with an ethylene rectifying tower condenser used for condensing a gas phase part on the top of the tower into a liquid phase, the bottom of the ethylene rectifying tower is connected with an ethylene rectifying tower reboiler used for gasifying a liquid phase part in a tower kettle, and heat exchange tubes of the ethylene rectifying tower condenser and the ethylene rectifying tower reboiler are provided with metal porous layers on the outer surface and/or the inner surface.

4. The methanol-to-olefin heat exchange system of claim 1, wherein: the rectifying tower (3) comprises a high-pressure depropanizing tower, the top of the high-pressure depropanizing tower is connected with a high-pressure depropanizing tower condenser used for condensing a gas phase part at the top of the tower into a liquid phase, the bottom of the high-pressure depropanizing tower is connected with a high-pressure depropanizing tower reboiler used for gasifying a liquid phase part at the bottom of the tower, and the outer surface and/or the inner surface of a heat exchange tube of the high-pressure depropanizing tower condenser are/is provided with a metal porous layer.

5. The methanol-to-olefin heat exchange system of claim 1, wherein: the rectifying tower (3) comprises a propylene rectifying tower, the top of the propylene rectifying tower is connected with a propylene rectifying tower condenser used for condensing a gas phase part on the top of the tower into a liquid phase, the bottom of the propylene rectifying tower is connected with a propylene rectifying tower reboiler used for gasifying a liquid phase part in a tower kettle, and a metal porous layer is arranged on the outer surface and/or the inner surface of a heat exchange tube of the propylene rectifying tower condenser.

6. The methanol-to-olefin heat exchange system of claim 1, wherein: the heat exchange tube of the propylene refrigerant condenser is characterized by further comprising a propylene refrigerant condenser, wherein the propylene refrigerant condenser is connected with a propylene machine and used for condensing gas-phase propylene at the outlet of the propylene machine into liquid-phase propylene, and a metal porous layer is arranged on the outer surface and/or the inner surface of the heat exchange tube of the propylene refrigerant condenser.