CN113440885B - Method and device for reducing temperature of low-pressure depropanizing tower kettle of ethylene device - Google Patents
Method and device for reducing temperature of low-pressure depropanizing tower kettle of ethylene device Download PDFInfo
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- CN113440885B CN113440885B CN202010226204.2A CN202010226204A CN113440885B CN 113440885 B CN113440885 B CN 113440885B CN 202010226204 A CN202010226204 A CN 202010226204A CN 113440885 B CN113440885 B CN 113440885B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
- B01D3/4211—Regulation; Control of columns
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/146—Multiple effect distillation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/08—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds
- C07C5/09—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds to carbon-to-carbon double bonds
Abstract
The invention belongs to the technical field of ethylene production devices in petrochemical industry, and discloses a method and a device for reducing the temperature of a low-pressure depropanizing tower kettle of an ethylene device, wherein the method comprises the following steps of; the tower kettle material of the low-pressure depropanizing tower is sent to a debutanizing tower, the tower top material of the debutanizing tower enters a debutanizing tower reflux tank after being cooled by a tower top condenser of the debutanizing tower, and the mixed carbon four in the debutanizing tower reflux tank is partially introduced into the low-pressure depropanizing tower through a debutanizing tower reflux/product pump so that the tower kettle temperature of the low-pressure depropanizing tower is controlled below 80 ℃. The method and the device can control the temperature of the kettle of the low-pressure depropanizing tower, so that the operation of the low-pressure depropanizing tower reaches the designed temperature, and the tower kettle can not cause the phenomena of coking and blockage of tower plates and a reboiler while ensuring the product purity.
Description
Technical Field
The invention belongs to the technical field of ethylene production devices in petrochemical industry, and particularly relates to a method and a device for reducing the temperature of a low-pressure depropanizing tower kettle of an ethylene device.
Background
A certain ethylene production device adopts a separation process of front depropanization and front hydrogenation, and a high-pressure depropanization tower and a cracked gas compressor form an open heat pump system at the inlet of a fifth section of the cracked gas compressor. The light key components of the process fluid of the high-pressure depropanizing tower are all carbon dioxide and partial carbon, and the heavy key components are carbon four and components heavier than carbon. The content of the carbon four components is strictly controlled at the tower top, because the excessive carbon four components can seriously affect the subsequent carbon two pre-hydrogenation system, so the tower top is generally controlled not to contain the carbon four or more components, and the tower bottom is controlled not to contain the carbon two or less components. During normal operation, the components in the tower bottom are three carbon components and components heavier than three carbon components. The tower bottom material flow is sent into a low-pressure depropanizing tower after being cooled. The top of the low-pressure depropanizing tower is controlled to contain no carbon four components, basically carbon three components, the bottom of the tower is controlled to contain no carbon three components, basically carbon four and components with more than carbon four, and the components are sent to a debutanizing tower for separation.
In an industrial application example, the overhead pressure of the low-pressure depropanizer is about 0.709MpaG, and the overhead temperature is 13.7 ℃. The column bottom pressure was about 0.752MPaG and the column bottom temperature was about 79.8 ℃. If the operation is improper during the production operation, the temperature of the tower bottom can exceed 80 ℃. At the moment, because the composition of the tower kettle is basically the components of carbon four and more than carbon four, when the temperature of the tower kettle exceeds 80 ℃, the carbon four unsaturated hydrocarbon components in the tower kettle can generate serious polymerization, the tower plate and a reboiler of the tower kettle can generate coking and blockage, the pressure difference of the tower is increased, the reboiler can not provide enough heating, and the device can be stopped in serious cases.
In many ethylene plant production operations, it is common practice to inject a suitable concentration of polymerization inhibitor at the low pressure depropanizer feed and reboiler inlet. The addition of inhibitors can mitigate coking of the trays and reboiler, but this approach tends to respond with lag, or sometimes less effective. This can affect the normal production operation of the ethylene plant.
Disclosure of Invention
In view of the above situation, the present invention aims to provide a method and an apparatus for reducing the temperature of a low-pressure depropanizing tower kettle of an ethylene plant, wherein the method can control the temperature of the tower kettle of the low-pressure depropanizing tower to be below 80 ℃ to ensure the separation effect of the low-pressure depropanizing tower.
A first aspect of the invention provides a method of reducing the temperature of a low pressure depropanizer drum of an ethylene plant, the method comprising; the tower kettle material of the low-pressure depropanizing tower is sent to a debutanizing tower, the tower top material of the debutanizing tower enters a debutanizing tower reflux tank after being cooled by a tower top condenser of the debutanizing tower, and the mixed carbon four in the debutanizing tower reflux tank is partially introduced into the low-pressure depropanizing tower through a debutanizing tower reflux/product pump so that the tower kettle temperature of the low-pressure depropanizing tower is controlled below 80 ℃.
The second aspect of the invention provides a device adopted by the method for reducing the temperature of the low-pressure depropanizing tower kettle of the ethylene device, the device comprises a low-pressure depropanizing tower and a debutanizing tower, a tower kettle discharge pipeline of the low-pressure depropanizing tower is connected with a feed inlet of the debutanizing tower, a first reflux pipeline is arranged at the tower top of the debutanizing tower, a debutanizing tower top condenser, a debutanizing tower reflux tank and a debutanizing tower reflux/product pump are sequentially arranged on the first reflux pipeline along the material flow direction, and a mixed carbon four extraction pipeline and a mixed carbon four introduction pipeline connected with the low-pressure depropanizing tower are arranged on a discharge pipeline of the debutanizing tower reflux/product pump.
The mixed carbon four introduction pipeline is additionally arranged on the low-pressure depropanizing tower, so that the aim of reducing the temperature of the low-pressure depropanizing tower kettle is fulfilled, the low-pressure depropanizing tower is stable in operation, the separation effect of the low-pressure depropanizing tower is ensured, the risk of coking and blockage of tower plates and a reboiler is reduced on the premise that tower kettle products and tower top products are qualified, and the device is safe and stable to operate in a long-term period.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention without limiting the invention.
FIG. 1 is a schematic of a prior art process for a low pressure depropanizer and debutanizer of an ethylene plant.
Figure 2 is a schematic process flow diagram for reducing the low pressure depropanizer drum temperature of an ethylene plant in accordance with an embodiment of the present invention.
Description of the reference numerals
1-a low pressure depropanizer; 2-a debutanizer column; 3-a debutanizer tower top condenser; 4-a debutanizer reflux drum; 5-debutanizer reflux/product pump; 6-mixed C4; 7-low pressure depropanizer reboiler; 8-a condenser at the top of the low-pressure depropanizer; 9-low pressure depropanizer reflux drum; 10-low pressure depropanizer reflux pump; 11-debutanizer reboiler; 12-crude pyrolysis gasoline; 13-a cooler; 14-mixed carbon four inlet line; 15-flow regulating valve; 16-flow meter.
Detailed Description
In order that the present invention may be more readily understood, the following detailed description of the invention is given with reference to the accompanying drawings and embodiments, which are given by way of illustration only and are not intended to limit the invention.
According to a first aspect of the invention, there is provided a process for reducing the temperature of a low pressure depropanizer drum of an ethylene plant, the process comprising; the tower kettle material of the low-pressure depropanizing tower is sent to a debutanizing tower, the tower top material of the debutanizing tower enters a reflux tank of the debutanizing tower after being cooled by a condenser at the tower top of the debutanizing tower, and the mixed carbon IV in the reflux tank of the debutanizing tower is partially introduced into the low-pressure depropanizing tower through a reflux/product pump of the debutanizing tower, so that the tower kettle temperature of the low-pressure depropanizing tower is controlled below 80 ℃.
In the invention, the introducing position of the mixed C4 on the low-pressure depropanizing tower can be a tower kettle, a stripping section, a rectifying section or other positions entering the tower, such as a feeding pipeline and the like.
According to the invention, the operating temperature of the reflux drum of the debutanizer is 43 ℃, and the mixed carbon four comprises 1,3-butadiene, 1-butene, isobutene, n-butane, isobutane.
Preferably, the amount of the mixed C.sub.four introduced is 30 to 50mol% of the total amount of C.sub.four components in the low pressure depropanizer. The specific introduction amount of the mixed C4 is adjusted according to the tower kettle temperature of the low-pressure depropanizing tower.
In the invention, the material flow in the high-pressure depropanizing tower is cooled by a cooler and then enters the low-pressure depropanizing tower. The condenser at the top of the low-pressure depropanizing tower adopts propylene refrigerant as a refrigerant. The temperature at the top of the low-pressure depropanizing tower is 13.7 ℃, and the temperature of the reflux tank of the low-pressure depropanizing tower is 10 ℃.
The process parameters which are not limited in the invention can be set conventionally according to the prior art, for example, the operation parameters of the low-pressure depropanizer and the debutanizer belong to the conventional technical means.
According to a second aspect of the present invention, the present invention provides an apparatus used in the method for reducing the temperature of the low-pressure depropanizing tower of the ethylene plant, the apparatus comprises a low-pressure depropanizing tower and a debutanizing tower, a tower bottom discharge pipeline of the low-pressure depropanizing tower is connected with a feed inlet of the debutanizing tower, a tower top of the debutanizing tower is provided with a first reflux pipeline, along a material flow direction, the first reflux pipeline is sequentially provided with a debutanizing tower top condenser, a debutanizing tower reflux tank and a debutanizing tower reflux/product pump, and a discharge pipeline of the debutanizing tower reflux/product pump is provided with a mixed four-carbon extraction pipeline and a mixed four-carbon introduction pipeline connected with the low-pressure depropanizing tower.
In the invention, the discharge end of the mixed C4 introducing pipeline is connected with a tower kettle, a stripping section, a rectifying section or a feeding pipeline of the low-pressure depropanizing tower.
Preferably, a flow meter and a flow regulating valve are arranged on the mixed carbon four introducing pipeline. And specifically adjusting the flow of the mixed carbon four according to the temperature of the low-pressure depropanizing tower kettle.
In the invention, the mixed C4 introducing pipeline is suitable in size, and cannot meet the requirement of long-period safe and stable operation when being too large or too small. The size of the mixed C4 introducing pipeline is not suitable to be too large so as to prevent excessive injection of the mixed C4, which causes the low temperature of the low-pressure depropanizing tower kettle, the content of light components in the tower kettle exceeds the standard, the separation effect of the tower is deteriorated, and the operation and the product quality are influenced. Similarly, the size of the mixed C4 introducing pipeline is not suitable to be too small, so as to prevent the phenomena of high temperature of the low-pressure depropanizing tower kettle, serious coking and blockage of the tower plate and the tower kettle reboiler and influence on the operation of the tower due to insufficient injection flow of the mixed C4 and unobvious effect. Preferably, the mixed carbon four introduction line has a size of 3".
According to the invention, a feeding pipeline is arranged at the upper part of the low-pressure depropanizing tower, a reboiler and a discharge pipeline are arranged at the tower kettle, a second return pipeline is arranged at the tower top, and a condenser at the tower top of the low-pressure depropanizing tower, a return tank of the low-pressure depropanizing tower and a return pump of the low-pressure depropanizing tower are sequentially arranged on the second return pipeline along the material flow direction.
In the invention, a feed inlet is arranged at the upper part of the debutanizer, a debutanizer reboiler and a crude pyrolysis gasoline discharge pipeline are arranged at the tower kettle, and a cooler is arranged on the crude pyrolysis gasoline discharge pipeline.
Components of the system which are not limited in the invention can be selected conventionally according to the prior art, and belong to the conventional technical means.
The invention provides a flexible adjustment means, which controls the kettle temperature of the low-pressure depropanizing tower by additionally arranging a mixed carbon four introduction pipeline, so that the operation of the low-pressure depropanizing tower reaches the designed temperature, and simultaneously, the separation effect of the low-pressure depropanizing tower is ensured. If the kettle temperature of the low-pressure depropanizing tower is too high in the production operation process, the operation of adjusting the opening degree of the valve on the added mixed C4 introducing pipeline is implemented to increase the flow of the C4 material flow and further reduce the temperature of the tower kettle of the low-pressure depropanizing tower. Even if the heating quantity of the reboiler is slightly increased in the production operation process, the tower kettle is not over-heated, so that the tower plate and the reboiler are not coked and blocked while the product purity of the tower kettle is ensured.
The present invention will be described in detail by way of examples.
Examples
This example illustrates the process and apparatus of the present invention for reducing the low pressure depropanizer drum temperature of an ethylene plant.
As shown in fig. 2, the present invention provides a method for reducing the low pressure depropanizer drum temperature of an ethylene plant, the method comprising; the tower kettle material of the low-pressure depropanizing tower 1 is sent to a debutanizing tower 2, the tower top material of the debutanizing tower 2 enters a debutanizing tower reflux tank 4 after being cooled by a debutanizing tower top condenser 3, part of mixed carbon four 6 in the debutanizing tower reflux tank 4 is introduced into the low-pressure depropanizing tower 1 through a debutanizing tower reflux/product pump 5, and the tower kettle temperature of the low-pressure depropanizing tower 1 is controlled below 80 ℃. The introducing position of the mixed carbon four 6 on the low-pressure depropanizing tower 1 is a tower kettle. The operating temperature of the debutanizer reflux drum 4 was 43 ℃, and the mixed carbon four 6 comprised 1,3-butadiene, 1-butene, isobutene, n-butane, isobutane. The introduced amount of the mixed C6 accounts for 30-50mol% of the total amount of the C four components in the low-pressure depropanizer 1.
The device adopted by the method for reducing the temperature of the low-pressure depropanizing tower kettle of the ethylene device comprises a low-pressure depropanizing tower 1 and a debutanizing tower 2, a tower kettle discharge pipeline of the low-pressure depropanizing tower 1 is connected with a feed inlet of the debutanizing tower 2, a first reflux pipeline is arranged at the tower top of the debutanizing tower 2, a debutanizing tower top condenser 3, a debutanizing tower reflux tank 4 and a debutanizing tower reflux/product pump 5 are sequentially arranged on the first reflux pipeline along the material flow direction, and a mixed carbon four 6 extraction pipeline and a mixed carbon four introduction pipeline 14 connected with the low-pressure depropanizing tower 1 are arranged on a discharge pipeline of the debutanizing tower reflux/product pump 5. The discharge end of the mixed carbon four introduction pipeline 14 is connected with the tower kettle of the low-pressure depropanizing tower 1. The mixed carbon four introducing pipeline 14 is provided with a flowmeter 16 and a flow regulating valve 15, the flow of the flow regulating valve is 12000kg/h normally, and the maximum flow is 15600kg/h. The mixed carbon four inlet line 14 has a size of 3".
The upper portion of low pressure depropanizing tower 1 is equipped with feed line, the tower cauldron is equipped with low pressure depropanizing tower reboiler 7 and tower cauldron discharge line, the top of the tower is equipped with second return line, along the material flow direction, be equipped with low pressure depropanizing tower top of the tower condenser 8, low pressure depropanizing tower reflux drum 9 and low pressure depropanizing tower reflux pump 10 on the second return line in proper order. The upper part of the debutanizer 2 is provided with a feed inlet, the tower kettle is provided with a debutanizer reboiler 11 and a crude pyrolysis gasoline 12 discharge pipeline, and the crude pyrolysis gasoline 12 discharge pipeline is provided with a cooler 13.
In the embodiment, a mixed C4 introducing pipeline 14 is led out from a reflux/product pump 5 of the debutanizer and is connected to the kettle position of the low-pressure depropanizer 1 to be used as a means for supplementing, adjusting and controlling the kettle temperature of the low-pressure depropanizer. Meanwhile, the mixed carbon four introduction line 14 is provided with a flow meter 16 and a flow regulating valve 15 for controlling the flow rate, and the opening degree of the valve is adjusted according to the temperature of the low-pressure depropanizing tower kettle. The condition that butadiene polymerization took place for the overtemperature easily appears in the low pressure depropanization tower cauldron during normal operation, when low pressure depropanization tower cauldron temperature rose, adjusted the regulating valve opening on the four inlet line of mixed carbon 14, increased the flow of four 6 of mixed carbon for the temperature of tower cauldron obtains control, and the operation of tower reaches the designing requirement.
The embodiment only takes the example of entering the tower bottom, and other positions for introducing the low-pressure depropanizer 1 are similar and are not listed.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the disclosed embodiments. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the illustrated embodiments.
Claims (7)
1. A method for reducing the temperature of a low-pressure depropanizer kettle of an ethylene plant, the method comprising; the tower kettle material of the low-pressure depropanizing tower is sent to a debutanizing tower, the tower top material of the debutanizing tower enters a debutanizing tower reflux tank after being cooled by a tower top condenser of the debutanizing tower, and the mixed carbon four in the debutanizing tower reflux tank is partially introduced into the low-pressure depropanizing tower through a debutanizing tower reflux/product pump so that the tower kettle temperature of the low-pressure depropanizing tower is controlled below 80 ℃;
wherein the introduction amount of the mixed C4 accounts for 30-50mol% of the total amount of the C four components in the low-pressure depropanizing tower;
the introduction position of the mixed carbon four on the low-pressure depropanizing tower is a tower kettle, a stripping section, a rectifying section or a feeding pipeline.
2. The method of reducing ethylene plant low pressure depropanizer kettle temperature of claim 1, wherein said debutanizer reflux drum operating temperature is 43 ℃ and said mixed carbon four comprises 1,3-butadiene, 1-butene, isobutene, n-butane, isobutane.
3. The apparatus used in the method for reducing the temperature of the low-pressure depropanizing tower kettle of the ethylene plant of claim 1 or 2 is characterized in that the apparatus comprises a low-pressure depropanizing tower and a debutanizing tower, a tower kettle discharge pipeline of the low-pressure depropanizing tower is connected with a feed inlet of the debutanizing tower, a first reflux pipeline is arranged at the tower top of the debutanizing tower, a debutanizing tower top condenser, a debutanizing tower reflux tank and a debutanizing tower reflux/product pump are sequentially arranged on the first reflux pipeline along the material flow direction, and a mixed four-carbon extraction pipeline and a mixed four-carbon introduction pipeline connected with the low-pressure depropanizing tower are arranged on a discharge pipeline of the debutanizing tower reflux/product pump;
wherein the discharge end of the mixed carbon four introduction pipeline is connected with a tower kettle, a stripping section, a rectifying section or a feeding pipeline of the low-pressure depropanizing tower.
4. The apparatus of claim 3, wherein the mixed carbon four inlet line is provided with a flow meter and a flow regulating valve.
5. The apparatus of claim 3, wherein the mixed carbon four introduction line is 3 "in size.
6. The device as claimed in claim 3, wherein the upper part of the low-pressure depropanizing tower is provided with a feeding pipeline, the tower kettle is provided with a low-pressure depropanizing tower reboiler and a tower kettle discharging pipeline, the tower top is provided with a second return pipeline, and the second return pipeline is sequentially provided with a low-pressure depropanizing tower top condenser, a low-pressure depropanizing tower return tank and a low-pressure depropanizing tower return pump along the material flow direction.
7. The apparatus of claim 3, wherein the upper part of the debutanizer is provided with a feed inlet, the tower bottom is provided with a debutanizer reboiler and a raw pyrolysis gasoline outlet line, and the raw pyrolysis gasoline outlet line is provided with a cooler.
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| CN103159581A (en) * | 2011-12-12 | 2013-06-19 | 中国石油化工股份有限公司 | System and method for preparing polymer-grade propylene through absorption and separation of catalytic cracking product gas |
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| US8586811B2 (en) * | 2012-02-17 | 2013-11-19 | Uop Llc | Processes and hydrocarbon processing apparatuses for preparing mono-olefins |
| CN108017499B (en) * | 2016-11-01 | 2021-02-05 | 中国石油化工股份有限公司 | Comprehensive utilization system and comprehensive utilization method for methanol-to-olefin reaction product |
| CN110388790B (en) * | 2019-07-31 | 2021-06-04 | 北京恒泰洁能科技有限公司 | Ethane cracking cryogenic separation process method |
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| CN103159581A (en) * | 2011-12-12 | 2013-06-19 | 中国石油化工股份有限公司 | System and method for preparing polymer-grade propylene through absorption and separation of catalytic cracking product gas |
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