CN215691754U - Separation system of sulfuric acid alkylation reaction product - Google Patents
Separation system of sulfuric acid alkylation reaction product Download PDFInfo
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- CN215691754U CN215691754U CN202121992751.8U CN202121992751U CN215691754U CN 215691754 U CN215691754 U CN 215691754U CN 202121992751 U CN202121992751 U CN 202121992751U CN 215691754 U CN215691754 U CN 215691754U
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Abstract
The utility model provides a separation system of sulfuric acid alkylation reaction products, which comprises a first rectifying tower (T1), a first reboiler (H1), a second rectifying tower (T2), a condenser (E1), a second reboiler (H2) and a third reboiler (H3); the first rectifying tower and the second rectifying tower are thermally coupled through an ascending steam pipeline and a reflux liquid pipeline. The raw material enters the first rectifying tower (T1) from the middle lower part thereof, qualified alkylate oil products are obtained by separating the bottom of the tower, qualified isobutane for circulation is obtained at the top of the second rectifying tower (T2), and qualified normal butane products are obtained at the bottom of the tower. Compared with the prior process flow, the separation system can reduce part of equipment and reduce occupied land; the second reboiler (H2) and the third reboiler (H3) can adopt low-quality condensed water or low-temperature hot water as a heat source, so that the use amount of high-quality heating media such as steam is saved, and the operation cost is reduced.
Description
Technical Field
The utility model relates to the technical field of petrochemical industry, in particular to a separation system for sulfuric acid alkylation reaction products.
Background
In the petroleum refining process, carbon four alkylation is an important process for processing refinery gas and is mainly used for producing high-octane gasoline blending components. The carbon four-alkylation device is an industrial facility which reacts isobutane and butene (or a mixture of propylene, butene and pentene) under the action of a catalyst to generate alkylate mainly comprising isooctane. The alkylate oil has the characteristics of high octane number, good antiknock property, low vapor pressure, low sulfur content, no olefin and aromatic hydrocarbon and the like, and is an ideal clean gasoline high-octane number blending component.
At present, the domestic alkylate production process mostly adopts a liquid acid catalysis process, namely, low-carbon olefin (including 1-butene, 2-butene, isobutene and the like) and isobutane are used as raw materials, the reaction is carried out under the catalysis of hydrofluoric acid or concentrated sulfuric acid, an alkylate product obtained after deacidification contains a large amount of unreacted isobutane and n-butane, n-butane and isobutane removal treatment needs to be carried out on the alkylate product, isobutane is used as a reaction raw material for recycling, so that the alkane-olefin ratio of a reaction system is increased, and the accumulation of n-butane in the reaction system is avoided.
Sulfuric acid alkylation was the earliest of the various carbon four alkylation technologies and is still widely used to date. Sulfuric acid used in the sulfuric acid alkylation technology is superior to hydrofluoric acid in safety, the problem of waste acid is well solved, and the requirement on high-octane gasoline blending components is rapidly increased along with the accelerated upgrading of gasoline quality in China in the 21 st century, so that the number and the processing capacity of sulfuric acid alkylation devices are rapidly developed in recent years.
The sulfuric acid alkylation unit mainly comprises five units: the device comprises a raw material pretreatment unit, an alkylation reaction unit, a compression refrigeration unit, a product fractionation unit and a chemical treatment unit. The product fractionation unit of the sulfuric acid alkylation device is a direct serial flow path consisting of two conventional rectifying towers and is used for separating alkylation reaction products, and the separation flow path is shown in figure 1. The isobutane for circulation is firstly obtained from the top of the rectifying tower T1, the product at the bottom of the tower enters the rectifying tower T2 by the pressure difference of the two towers, the qualified normal butane product is obtained at the top of the tower, and the qualified alkylate oil product is obtained at the bottom of the tower. The temperature of the tower bottom of the two towers is above 100 ℃, and the energy consumption mainly comes from 1.0MPa steam consumed by the two tower reboilers. Since steam is a high quality heating medium, the operating costs of the plant are high.
The alkylation product separation device disclosed in the Chinese patent CN205170706U has the disadvantages of complex flow, high equipment cost, large occupied area and the like. The alkylated product separation system disclosed in chinese patents CN206521436U and CN208287526U has a vertical baffle installed in the middle of the rectifying tower, which divides the rectifying tower into four parts, namely a common rectifying section, a common stripping section, a pre-rectifying section and a side draw section, and has the problems of suitability, limited energy saving effect, and high operating cost because the heating medium of the reboiler in the tower needs to be completely high-quality heat sources such as low-pressure steam.
In view of this, the present application is presented.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a separation system of sulfuric acid alkylation reaction products, which aims to simplify the process flow, reduce the number of equipment and the occupied area and reduce the operation cost through heat coupling.
The technical scheme of the utility model is summarized as follows:
a separation system of sulfuric acid alkylation reaction products comprises a first rectifying tower (T1), a first reboiler (H1), a second rectifying tower (T2), a condenser (E1) and a second reboiler (H2); the alkylation reaction product raw material pipeline is connected with a raw material feeding port of a first rectifying tower (T1), and a liquid phase material discharging port at the bottom of the first rectifying tower (T1) is connected with an alkylate oil discharging pipeline; the liquid phase inlet of the first reboiler (H1) is connected with the tower bottom of the first rectifying tower (T1), and the outlet of the first reboiler (H1) is connected with the tower body of the first rectifying tower (T1); a gas-phase material discharge port at the top of the first rectifying tower (T1) is connected with a feed port of a second rectifying tower (T2), and a reflux liquid discharge port above the feed port of the second rectifying tower (T2) is connected with a liquid-phase material reflux port at the top of the first rectifying tower (T1); the top steam outlet of the second rectifying tower (T2) is connected with the inlet of a condenser (E1), the outlet pipeline of the condenser (E1) is divided into two parts, one part is connected to the liquid phase material reflux port of the second rectifying tower (T2), and the other part is used as a discharge pipeline of the isobutane for circulation; the liquid phase inlet of a second reboiler (H2) is connected with the tower kettle of a second rectifying tower (T2) through a pipeline, and the outlet of the second reboiler (H2) is connected with the tower body of the second rectifying tower (T2); the liquid phase material outlet at the bottom of the second rectifying tower (T2) is connected with a normal butane outlet pipeline.
When utility conditions are met, the separation apparatus may further comprise a third reboiler (H3); the third reboiler (H3) is positioned at the middle upper part of the stripping section of the first rectifying tower (T1) of the third reboiler (H3), the feed inlet of the third reboiler (H3) is used for conveying the liquid-phase material in the first rectifying tower (T1) to the third reboiler (H3), and the discharge outlet of the third reboiler (H3) is used for conveying the material back to the first rectifying tower (T1).
The separation device is suitable for the separation of sulfuric acid alkylation reaction products, and is also suitable for the separation process of separating a mixture consisting of two similar light hydrocarbons with similar boiling points and heavy hydrocarbons (or heavy components) to obtain three products.
The embodiment of the utility model has the beneficial effects that:
compared with the prior art, the utility model reduces the condensers, reflux tanks, reflux pumps and the like at the top of the first rectifying tower, and reduces the occupied area. Meanwhile, the temperature of a reboiler at the bottom of the second rectifying tower and the temperature of a reboiler in the middle of the stripping section of the first rectifying tower are lower, and low-quality condensed water or low-temperature hot water can be used as a heat source, so that the consumption of high-quality heat sources such as steam is saved, and the operation cost is reduced.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some embodiments of the present invention and therefore should not be considered as limiting the scope, and for those skilled in the art, other related drawings can be obtained from the drawings without inventive efforts.
FIG. 1 is a flow diagram of the separation of the product of a sulfuric acid alkylation reaction in the prior art;
FIG. 2 is a flow diagram of a sulfuric acid alkylation reaction product separation system provided in example 1 of the present invention;
FIG. 3 is a flow diagram of a sulfuric acid alkylation reaction product separation system provided in example 2 of the present invention.
The reference numbers: a first rectification column-T1; a second rectification column-T2; condenser-E1; a first reboiler-H1; a second reboiler-H2; third reboiler-H3.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be described more clearly and completely with reference to the drawings in the embodiments of the present invention.
It is to be understood that the described embodiments are only some, but not all, embodiments of the utility model. The components of embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations. Thus, the following detailed description of the embodiments of the present invention, presented in the figures, is not intended to limit the scope of the utility model, as claimed, but is merely representative of selected embodiments of the utility model. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The terms "first," "second," and the like are used solely to distinguish one from another and are not to be construed as indicating or implying relative importance. Furthermore, the terms "horizontal", "vertical" and the like do not imply that the components are required to be absolutely horizontal or pendant, but rather may be slightly inclined. For example, "horizontal" merely means that the direction is more horizontal than "vertical" and does not mean that the structure must be perfectly horizontal, but may be slightly inclined.
In the description of the present invention, it should also be noted that, unless otherwise explicitly specified or limited, the terms "disposed," "mounted," "connected," and "connected" are to be construed broadly and may, for example, be fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood as appropriate by those of ordinary skill in the art.
The utility model provides a separation system of sulfuric acid alkylation reaction products, which is used for separating the sulfuric acid alkylation reaction products. The specific implementation is as follows:
the sulfuric acid alkylation reaction product separation device shown in fig. 2 provided by the utility model can be adopted, and comprises a first rectifying tower (T1), a first reboiler (H1), a second rectifying tower (T2), a condenser (E1) and a second reboiler (H2). The alkylation reaction product raw material pipeline is connected with a raw material feeding port of a first rectifying tower (T1), and a liquid phase material discharging port at the bottom of the first rectifying tower (T1) is connected with an alkylate oil discharging pipeline; the liquid phase inlet of the first reboiler (H1) is connected with the tower bottom of the first rectifying tower (T1), and the outlet of the first reboiler (H1) is connected with the tower body of the first rectifying tower (T1); a gas-phase material discharge port at the top of the first rectifying tower (T1) is connected with a feed port of a second rectifying tower (T2), and a reflux liquid discharge port above the feed port of the second rectifying tower (T2) is connected with a liquid-phase material reflux port at the top of the first rectifying tower (T1); the top steam outlet of the second rectifying tower (T2) is connected with the inlet of a condenser (E1), the outlet pipeline of the condenser (E1) is divided into two parts, one part is connected to the liquid phase material reflux port of the second rectifying tower (T2), and the other part is used as the discharge pipeline of the isobutane for circulation. The liquid phase inlet of a second reboiler (H2) is connected with the tower kettle of a second rectifying tower (T2) through a pipeline, and the outlet of the second reboiler (H2) is connected with the tower body of the second rectifying tower (T2); the liquid phase material outlet at the bottom of the second rectifying tower (T2) is connected with a normal butane outlet pipeline.
When a low-quality heat source (a low-temperature heat source such as heat medium water or condensed water) is abundant, the separation system may further include a third reboiler H3, see fig. 3; the third reboiler (H3) is positioned at the middle upper part of the stripping section of the first rectifying tower (T1) of the third reboiler (H3), the feed inlet of the third reboiler (H3) is used for conveying the liquid-phase material in the first rectifying tower (T1) to the third reboiler (H3), and the discharge outlet of the third reboiler (H3) is used for conveying the material back to the first rectifying tower (T1).
In specific implementation, the theoretical plate number of the first rectifying tower T1 is 20-60, and the theoretical plate number of the second rectifying tower T2 is 30-100. The two conventional rectifying towers can be plate towers, packed towers or any combination of the two towers, and the types of the two towers can be the same or different.
In specific implementation, when cooling water is used as a cooling medium, the top temperature of the second rectifying tower T2 is 40-60 ℃, the top pressure is 0.42-0.6MPa (g), the bottom temperature of the first rectifying tower T1 is higher than 80 ℃, and the bottom temperature of the second rectifying tower T2 is 50-70 ℃.
In specific implementation, the heating medium of the first reboiler H1 may be low-pressure steam, heat transfer oil, or the like, and the heating medium of the second reboiler H2 and the third reboiler H3 may be low-temperature hot water such as low-pressure steam, heat transfer oil, condensed water, or heat transfer water, and preferably a low-temperature and low-cost heat source such as heat transfer water or condensed water.
In specific implementation, when the feed composition contains light components, the top of the tower can extract non-condensable components, and the isobutane outlet is positioned at the position of 2-10 trays below the top of the partition rectifying tower T1.
In the specific implementation, when a high-grade cooling medium is adopted, the operation can be carried out under normal pressure or reduced pressure, and the separation process and the device can still be used. The separation operating conditions are determined by the composition and the specific cooling medium conditions.
The features and properties of the present invention are described in further detail below with reference to examples.
Taking an alkylation unit of 20 ten thousand tons/year in a certain refinery as an example, the sulfuric acid alkylation reaction product is separated by using the examples and the comparative examples, the recycling isobutane is required to reach 90 percent in mole fraction, the normal butane product reaches 99 percent in mole fraction, and the normal butane content in the alkylate oil product does not exceed 500 ppm.
Example 1
In this example, the separation device provided by the present invention is used for separation, and the process flow shown in fig. 2 is used.
The heating medium of the first reboiler H1 was saturated steam at 1.0MPa, and the price was 200 Yuan/ton. The heating medium of the second reboiler H2 adopts condensed water, the price is calculated by 10 yuan/ton, the inlet temperature is 110 ℃, and the outlet temperature is 65 ℃. The cooling medium of the condenser E1 was circulated cooling water and the price was 0.2 Yuan/ton. The inlet temperature was 30 ℃ and the outlet temperature was 40 ℃.
The sulfuric acid alkylation reaction product raw material is fed from the optimized position on the left side of the partition plate at the mass flow rate of 65800kg/h under the bubble point state, and the product quality is completely qualified by adopting a proper tower structure and optimized operation conditions.
Through calculation: the steam consumption of the first reboiler H1 was 11.36 tons/hr, the condensed water consumption of the second reboiler H2 was 176.37 tons/hr, and the cooling water consumption of the condenser E1 was 1274.57 tons/hr, and the total operating cost was 4290.2 yuan/hr.
Example 2
The separation is carried out by adopting the preferred mode of the thermal coupling and heat pump combined separation process, and the process flow shown in the figure 3 is adopted. The heating medium of the third reboiler H3 adopts condensed water, and the inlet temperature is 110 ℃ and the outlet temperature is 70 ℃.
Through calculation: the steam consumption of the first reboiler H1 was 9.07 ton/hr, the condensate consumption of the second reboiler H2 was 176.37 ton/hr, the condensate consumption of the third reboiler H3 was 30.01 ton/hr, and the cooling water consumption of the condenser E1 was 1274.57 ton/hr, and the total operating cost was 4132.2 yuan/hr.
Comparative example 1
The process flow of the existing conventional rectifying tower direct sequence separation is adopted, and the whole process comprises two conventional rectifying towers as shown in figure 1.
The raw material of the sulfuric acid alkylation reaction product enters a separation device at a mass flow rate of 65800kg/h in a bubble point state, and the product quality is completely qualified by adopting a proper tower structure and optimizing operation conditions.
Through calculation: the steam consumption of the rectifying tower T1 is 20.59 tons/hour, and the steam consumption of the rectifying tower T2 is 3.42 tons/hour; the cooling water consumption of the rectifying tower T1 is 1066.32 tons/hour, and the cooling water consumption of the rectifying tower T2 is 148.02 tons/hour; the aggregate operating cost was 5016.5 dollars/hour.
The operating costs of example 1, example 2 and comparative example 1 were compared as shown in table 1:
TABLE 1 operating expense test results
| Contrast item | Comparative example 1 | Example 1 | Example 2 |
| Operating expenses (Yuan/Shi) | 5016.5 | 4290.2 | 4132.2 |
As can be seen from the above table: compared with the comparative example 1 which adopts the prior separation process of the conventional rectifying tower in a direct sequence mode, the operation cost of the example 1 which adopts the novel separation device provided by the embodiment of the utility model to carry out separation is obviously reduced. If the preferred embodiment of example 2 is used, an intermediate reboiler is added, further saving operating costs.
The above is only a preferred embodiment of the present invention, and is not intended to limit the present invention, and various modifications and changes will occur to those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (5)
1. A separation system of sulfuric acid alkylation reaction products is characterized by comprising a first rectifying tower (T1), a first reboiler (H1), a second rectifying tower (T2), a condenser (E1) and a second reboiler (H2); the alkylation reaction product raw material pipeline is connected with a raw material feeding port of a first rectifying tower (T1), and a liquid phase material discharging port at the bottom of the first rectifying tower (T1) is connected with an alkylate oil discharging pipeline; the liquid phase inlet of the first reboiler (H1) is connected with the tower bottom of the first rectifying tower (T1), and the outlet of the first reboiler (H1) is connected with the tower body of the first rectifying tower (T1); a gas-phase material discharge port at the top of the first rectifying tower (T1) is connected with a feed port of a second rectifying tower (T2), and a reflux liquid discharge port above the feed port of the second rectifying tower (T2) is connected with a liquid-phase material reflux port at the top of the first rectifying tower (T1); the top steam outlet of the second rectifying tower (T2) is connected with the inlet of a condenser (E1), the outlet pipeline of the condenser (E1) is divided into two parts, one part is connected to the liquid phase material reflux port of the second rectifying tower (T2), and the other part is used as a discharge pipeline of the isobutane for circulation; the liquid phase inlet of a second reboiler (H2) is connected with the tower kettle of a second rectifying tower (T2) through a pipeline, and the outlet of the second reboiler (H2) is connected with the tower body of the second rectifying tower (T2); the liquid phase material outlet at the bottom of the second rectifying tower (T2) is connected with a normal butane outlet pipeline.
2. The separation system of claim 1, further comprising a third reboiler (H3); the third reboiler (H3) is positioned at the middle upper part of the stripping section of the first rectifying tower (T1) in the third reboiler (H3), the feed inlet of the third reboiler (H3) is used for conveying the liquid-phase material in the first rectifying tower (T1) to the third reboiler (H3), and the discharge outlet is used for conveying the material from the third reboiler (H3) back to the first rectifying tower (T1).
3. The separation system according to claim 1, wherein the theoretical plate number of the first rectification column (T1) is 20 to 60, and the theoretical plate number of the second rectification column (T2) is 30 to 100.
4. The separation system of claim 1, wherein the two conventional rectification columns are plate columns, packed columns, or any combination thereof.
5. The separation system of claim 1, wherein when the feed composition contains light components, the non-condensable components are extracted from the top of the tower, and the isobutane outlet is positioned 2-10 trays below the top of the partition rectifying tower T1.
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| CN202121992751.8U CN215691754U (en) | 2021-08-23 | 2021-08-23 | Separation system of sulfuric acid alkylation reaction product |
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