CN216062074U - Separation device for alkylation reaction product - Google Patents
Separation device for alkylation reaction product Download PDFInfo
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- CN216062074U CN216062074U CN202121992646.4U CN202121992646U CN216062074U CN 216062074 U CN216062074 U CN 216062074U CN 202121992646 U CN202121992646 U CN 202121992646U CN 216062074 U CN216062074 U CN 216062074U
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Abstract
The utility model discloses a separation device of alkylation reaction products, which is a process technology for separating isobutane for circulation, high-purity n-butane and qualified alkylate oil products from sulfuric acid alkylation reaction products by adopting a separation process combining a conventional rectification two-tower indirect sequence and a heat pump technology. And the alkylation reaction product is used as a raw material to enter a rectifying tower T1, a qualified alkylate oil product is extracted from the bottom of the tower, a liquid phase product at the top of the tower is used as a raw material to enter a rectifying tower T2, a qualified normal butane product is extracted from the bottom of the rectifying tower T2, and qualified isobutane for circulation is obtained at the top of the tower. The tower top steam of the rectifying tower T2 is pressurized and heated by a steam compressor and is used as a heat source of a reboiler at the tower bottom of the rectifying tower T2, and the auxiliary reboiler H3 is used for further providing required heat for the tower bottom liquid phase. When the separation index which is the same as that of the existing process flow is obtained, the process can be used for obviously reducing the energy consumption of the whole separation process, and has obvious practicability and technical economy.
Description
Technical Field
The utility model relates to the field of petrochemical industry, in particular to a separation device for 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. One of the major problems of the current sulfuric acid alkylation unit is high energy consumption, which is about 138.2kg standard oil per ton raw material, wherein the energy consumption of the fractionation part accounts for about 55% of the total energy consumption of the unit.
The product fractionation unit of the sulfuric acid alkylation unit is a direct sequence flow composed of two conventional rectification towers for separating the alkylation reaction products, and the separation flow is shown in fig. 3. 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 ℃, the energy consumption mainly comes from 1.0MPa steam consumed by the two tower reboilers, and the two fractionating towers consume about 1.0MPa steam per hour by taking 20 ten thousand tons/year of sulfuric acid alkylation equipment as an example.
A Heat Pump (Heat Pump) is a device for transferring Heat energy from a low-level Heat source to a high-level Heat source, and is also a new energy technology which attracts attention worldwide. The heat pump rectification is to heat up the steam at the top of the tower after the steam is adiabatically compressed by a compressor and then is used as a heat source of a reboiler again, the condensation latent heat of the steam at the top of the tower is recovered, a cold fluid is partially vaporized, and the compressed gas is condensed into liquid; after passing through the throttle valve, one part of the condensate is taken as the distillate at the top of the tower for extraction, and the other part of the condensate is returned to the top of the tower to be taken as the reflux. Apart from the start-up phase, essentially no additional heat can be supplied to the tower bottom reboiler, so that heat pump rectification is a good energy-saving technology. The heat pump rectification has a certain application range, and whether the heat pump rectification is used or not is determined by accurate economic evaluation according to the process requirement of a rectification tower.
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 utility model is particularly proposed.
SUMMERY OF THE UTILITY MODEL
The present invention is directed to overcoming the above-mentioned deficiencies of the prior art by providing an apparatus for the separation of alkylation reaction products.
The utility model provides a separation process of alkylation reaction products, wherein the alkylation reaction products are used as raw materials to enter a first rectifying tower for separation, qualified alkylate oil products are obtained at the bottom of the tower, and liquid phase products at the top of the tower are used as raw materials to enter a second rectifying tower for separation; and obtaining a qualified isobutane product for circulation at the top of the second rectifying tower and a qualified normal butane product at the bottom of the second rectifying tower. And (2) pressurizing the top steam of the second rectifying tower by using a steam compressor to increase the temperature, using the pressurized top steam as a heat source of a reboiler at the bottom of the second rectifying tower, completely liquefying the heat exchanged with the liquid phase in the tower kettle, reducing the pressure and cooling the heat through an adjusting valve (or other pressure reducing equipment), partially vaporizing the heat, condensing the heat to completely change the heat into the liquid phase, returning a part of the liquid phase into the tower as reflux liquid of the second rectifying tower, and extracting a part of the liquid phase as circulating isobutane. And an auxiliary reboiler is arranged at the bottom of the second rectifying tower to further provide required heat for the liquid phase in the tower kettle. When the heat medium water or the condensed water is provided, the stripping section of the first rectifying tower is provided with an intermediate reboiler.
The utility model is realized by the following steps:
the utility model provides a separation device of an alkylation reaction product, which comprises a first rectifying tower, a first reboiler, a first condenser, a second rectifying tower, a second reboiler, a third reboiler, a second condenser, a steam compressor and a regulating valve; the alkylation reaction product raw material pipeline is connected with a raw material feeding port of the first rectifying tower, and a liquid phase material discharging port at the bottom of the first rectifying tower is connected with an alkylate oil discharging pipeline; the liquid phase inlet of the first reboiler is connected with the tower kettle of the first rectifying tower, and the outlet of the first reboiler is connected with the tower body of the first rectifying tower; a gas-phase material discharge port at the top of the first rectifying tower is connected with a feed port of the first condenser, so that the gas-phase material is completely condensed in the first condenser, an outlet pipeline of the first condenser is divided into two parts, one part of condensate is connected to a liquid-phase material reflux port at the top of the first rectifying tower, the other part of condensate is connected to a raw material feed port of the second rectifying tower, a gas-phase material extraction port at the top of the second rectifying tower is connected with an inlet of a steam compressor, an outlet of the steam compressor is connected with a heat source inlet of a second reboiler at a tower kettle of the second rectifying tower, a heat source outlet of the second reboiler is connected with an inlet of an adjusting valve, an outlet of the adjusting valve is connected with an inlet of the second condenser, an outlet pipeline of the second condenser is divided into two parts, one part is used as a discharge pipeline for recycling isobutane, and the other part is connected with a liquid-phase material reflux port of the second rectifying tower; the liquid phase inlet of the second reboiler is connected with the tower kettle of the second rectifying tower through a pipeline, and the outlet of the second reboiler is connected with the tower body; a liquid phase inlet of the third reboiler is connected with the tower kettle of the second rectifying tower, and an outlet of the third reboiler is connected with the tower body of the second rectifying tower; and a liquid-phase material discharge port at the bottom of the second rectifying tower is connected with a normal butane discharge pipeline.
In a preferred embodiment of the present invention, the separation apparatus may further include a fourth reboiler H4, the fourth reboiler H4 is located at an upper middle portion of the stripping section of the first rectification column T1, a feed inlet of the fourth reboiler H4 is configured to feed the liquid-phase material in the first rectification column T1 to the fourth reboiler H4, and a discharge outlet of the fourth reboiler H4 is configured to feed the vapor-liquid mixture material from the fourth reboiler H4 back to the first rectification column T1.
The utility model has the following beneficial effects:
the utility model aims to provide a novel separation and purification process combining a conventional rectification two-tower indirect sequence and a heat pump technology, and the separation of sulfuric acid alkylation reaction products is realized. By utilizing the process method provided by the utility model, the same separation index as the existing process is obtained, and simultaneously, the energy consumption of the whole separation process can be obviously reduced, compared with the embodiment, the heat load can be reduced by 28 percent, and the cold load can be reduced by more than 45 percent.
In the case where the condensate water or the heat medium water is provided, the fourth reboiler H4 can further reduce the consumption of the high-quality heating medium in the first reboiler H1, and further reduce the operation cost, and thus the method has significant practicability and technical economy.
Drawings
In order to more clearly illustrate the technical solution of the embodiment of the present invention, the drawings needed to be used in the embodiment will be briefly described below, it should be understood that the following drawings only show the main equipment and pipelines of the apparatus 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 according to the drawings without creative efforts.
FIG. 1 is a schematic diagram of a separation device for separating alkylate by using a conventional two-tower indirect rectification sequence and heat pump combined process without an intermediate reboiler in example 1 of the present invention;
FIG. 2 is a schematic diagram of a separation device provided with an intermediate reboiler for separating alkylate by using a conventional two-tower indirect rectification sequence and heat pump combined process in example 2 of the present invention;
FIG. 3 is a schematic diagram of a prior art process for the separation of alkylate in the sulfuric acid alkylation fractionation unit of comparative example 1;
the reference numbers: the system comprises a first rectifying tower-T1, a second rectifying tower-T2, a first condenser-E1, a second condenser-E2, a first reboiler-H1, a second reboiler-H2, a third reboiler-H3, a fourth reboiler-H4, a vapor compressor-C1 and a regulating valve-V1.
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 below. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer.
The utility model provides a separation process combining an indirect sequence of two towers of conventional rectification and a heat pump, which is used for realizing the separation of sulfuric acid alkylation reaction products. The specific embodiments of the present invention are such that:
example the present invention may be used to provide an apparatus for the separation of the alkylation reaction product as shown in figure 1. The separation device comprises a first rectifying tower T1, a first reboiler H1, a first condenser E1, a second rectifying tower T2, a second reboiler H2, a third reboiler H3, a second condenser E2, a vapor compressor C1 and an adjusting valve V1; the alkylation reaction product raw material pipeline is connected with a raw material feeding hole of a first rectifying tower T1, and a liquid-phase material discharging hole at the bottom of the first rectifying tower T1 is connected with an alkylate oil discharging pipeline; a liquid phase inlet of the first reboiler H1 is connected with the tower bottom of the first rectifying tower T1, and an outlet of the first reboiler H1 is connected with the tower body of the first rectifying tower T1; a gas-phase material outlet at the top of the first rectifying tower T1 is connected with a feed inlet of the first condenser E1, so that the gas-phase material is completely condensed in the first condenser E1, an outlet pipeline of the first condenser E1 is divided into two parts, one part of condensate is connected to a liquid-phase material reflux port at the top of the first rectifying tower T1, the other part of condensate is connected to a raw material feed port of the second rectifying tower T2, a gas-phase material extraction port at the top of the second rectifying tower T2 is connected with an inlet of a vapor compressor C1, an outlet of the vapor compressor C1 is connected with a second reboiler H2 heat source inlet at the bottom of the second rectifying tower T2, a second reboiler H2 heat source outlet is connected with an inlet of a regulating valve V1, an outlet of the regulating valve V1 is connected with an inlet of the second condenser E2, an outlet pipeline of the second condenser E2 is divided into two parts, one part serves as a recycling isobutane discharge pipeline, and the other part is connected with a liquid-phase material reflux port of the second rectifying tower T2; a liquid phase inlet of a second reboiler H2 is connected with a tower kettle of a second rectifying tower T2 through a pipeline, and an outlet of the second reboiler H2 is connected with a tower body; a liquid phase inlet of a third reboiler H3 is connected with the tower kettle of the second rectifying tower T2, and an outlet of the third reboiler H3 is connected with the tower body of the second rectifying tower T2; the liquid phase material discharge port at the bottom of the second rectifying tower T2 is connected with a normal butane discharge pipeline.
In a preferred embodiment of the present invention, when the utility conditions are met, the separation apparatus may further include a fourth reboiler H4, the fourth reboiler H4 is located at the middle-upper portion of the stripping section of the first fractionator T1, the feed inlet of the fourth reboiler H4 is used for feeding the liquid-phase material in the first fractionator T1 to the fourth reboiler H4, and the discharge outlet is used for feeding the vapor-liquid mixture material from the fourth reboiler H4 back to the first fractionator T1.
In specific implementation, the number of trays of the first rectifying tower T1 is 30-80, preferably 50-60, and the number of trays of the second rectifying tower T2 is 50-110, preferably 65-80. 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, 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 ℃. The top temperature of the second rectifying tower T2 is 40-60 ℃, and the top pressure is 0.42-0.6MPa (g).
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, the third reboiler H3, or the fourth reboiler H4 may be low-pressure steam, heat transfer oil, condensed water, heat transfer water, or the like, and low-temperature and low-cost heat sources such as heat transfer water and condensed water are preferable.
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 raw material composition is shown in the following table 1, the recycling isobutane mole fraction is required to reach 90%, the n-butane product mole fraction is required to reach 99%, and the n-butane content in the alkylate oil product is not more than 500 ppm.
TABLE 1
Example 1
In the embodiment, a conventional rectification two-tower indirect sequence and heat pump combined process is adopted for separation, and a process flow shown in figure 1 is adopted. The heating medium of the first reboiler H1 was saturated steam at 1.0MPa, and the price was 200 Yuan/ton. The cooling medium of the condenser is circulated cooling water, and the price is 0.2 yuan/ton. The inlet temperature was 30 ℃ and the outlet temperature was 40 ℃.
In the examples, the sulfuric acid alkylation reaction product feed was fed from the lower middle portion of the first rectification column T1 at a mass flow rate of 65800kg/h under bubble point conditions, with the bottom temperature of the first rectification column T1 being 159.9 ℃, the top temperature of the second rectification column T2 being 43.2 ℃, the bottom temperature being 56.8 ℃ and the top pressure being 0.46mpa (g). The product quality reaches the standard and is fully optimized, and the calculation result is as follows:
the heating quantity of a reboiler H1 at the bottom of the first rectifying tower T1 is 6823.12kw, and the steam consumption is 11.16 tons/hour. The heating quantity of the auxiliary reboiler H3 is 1130.32kw, and the steam consumption is 1.83 ton/H.
The power consumption of the steam compressor C1 is 1120.46kw, the reduced energy consumption of heat energy is 2801.15kw, and the reduced steam consumption is 4.58 tons/hour.
The energy consumption of the condenser E1 was-5503.15 kw, and the circulating cooling water consumption was 475.05 tons/hr. The energy consumption of the condenser E2 was-2110.04 kw, and the circulating cooling water consumption was 182.15 tons/hr.
Example 2
In the embodiment, the separation is carried out by adopting a conventional two-tower indirect sequence of rectification and a heat pump combined process, and an intermediate reboiler H4 is added in a stripping section of a first rectification tower T1, as shown in figure 2. The heating media of the auxiliary reboiler H3 and the intermediate reboiler H4 adopt condensed water, the price is 10 yuan/ton, the inlet temperature is 110 ℃, and the outlet temperature is 70 ℃. The calculation result after the product quality reaches the standard is as follows:
the heating quantity of a reboiler H1 at the bottom of the first rectifying tower T1 is 5333.38kw, the steam consumption is 8.72 tons/hour, the heating quantity of an auxiliary reboiler H3 is 1130.32kw, the condensed water is consumed for 24.22 tons/hour, the heating quantity of an intermediate reboiler H4 is 1500kw, and the condensed water is consumed for 32.15 tons/hour.
The power consumption of the steam compressor C1 is 1120.46kw, calculated as 40% thermoelectric efficiency, reduced thermal energy consumption 2801.15kw, reduced steam consumption is 4.58 tons/hr.
The energy consumption of the condenser E1 was-5513.38 kw, and the circulating cooling water consumption was 475.94 tons/hr. The energy consumption of the condenser E2 was-2110.04 kw, and the circulating cooling water consumption was 182.15 tons/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 3.
The sulfuric acid alkylation reaction product raw material enters a rectifying tower T1 from a proper position at a mass flow rate of 65800kg/h under a bubble point state, and the tower top distillate is circulating isobutane with the mole fraction of 90%. The distillate at the bottom of the rectifying tower T1 enters the rectifying tower T2 by means of autogenous pressure, the distillate at the top of the tower is a normal butane product, and the mole fraction of the normal butane product is 99 percent; the distillate from the bottom of the tower is alkylate product with n-butane content of 500 ppm. The calculation result after the flow is fully optimized is as follows:
the heating quantity of the bottom of the rectifying tower T1 is 12819.92kw, the steam consumption is 20.59 ton/hr, the heating quantity of the bottom of the rectifying tower T2 is 2131.46kw, and the steam consumption is 3.42 ton/hr.
The energy consumption of the overhead condenser of the rectifying tower T1 is-12369.57 kw, and the circulating cooling water consumption is 1067.79 tons/hour. The energy consumption of the overhead condenser of the rectifying tower T2 is-1703.92 kw, and the circulating cooling water consumption is 146.91 tons/hour.
The energy consumption results of example 1 and comparative example 1 were compared as shown in table 2:
TABLE 2
As can be seen from table 2: compared with the comparative example 1 which adopts the conventional direct sequence mode of the conventional rectifying tower to carry out separation, the example 1 which adopts the novel separation process provided by the utility model to carry out separation obviously saves energy consumption. Accounting to the whole device, the energy consumption of the whole sulfuric acid alkylation device is reduced by about 15 percent.
The operating costs of example 1 and comparative example 1 were compared as shown in table 3:
TABLE 3
| Category of public works | Comparative example 1 | Example 1 | Saving value | Price (Yuan/ton) | Saving cost (Yuan/h) |
| 1.0MPa steam consumption (T/h) | 24.01 | 17.58 | 6.43 | 200 | 1286 |
| Consumption of cooling water (T/h) | 1214.88 | 657.20 | 557.68 | 0.2 | 111.54 |
| Total up to | 1397.54 |
As can be seen from table 3 above: compared with the comparative example 1 which adopts the prior conventional rectifying tower to carry out direct sequence separation, the example 1 which adopts the novel separation process provided by the utility model to carry out separation obviously saves the operation cost.
The energy savings of example 2 and comparative example 1 were compared in terms of operating costs, as shown in table 4:
TABLE 4
| Category of public works | Comparative example 1 | Example 2 | Saving value | Price (Yuan/ton) | Saving cost (Yuan/h) |
| 1.0MPa steam consumption (T/H) | 24.01 | 13.3 | 10.71 | 200.00 | 2142 |
| Consumption of condensate (T/H) | 0 | 56.37 | -56.37 | 10 | -563.7 |
| Consumption of Cooling Water (T/H) | 1214.88 | 658.09 | 556.79 | 0.20 | 111.36 |
| Total up to | 1689.66 |
As can be seen from table 4 above: compared with the comparative example 1 which adopts the prior conventional rectifying tower to carry out direct sequence separation, the example 2 which adopts the preferred mode of the novel separation process provided by the utility model to carry out separation greatly saves the operation cost. As can be seen by comparing Table 3 with Table 4, after the intermediate reboiler is added, the condensed water is used as the heating medium, thereby further saving the operation cost.
Comparing example 1 with comparative example 1, the new device provided by the utility model adds a 1200kw reciprocating compressor, throttle valve, auxiliary reboiler, etc., increases the tower height, tower diameter and other equipment investment, the total investment increase is estimated to be about 800 ten thousand yuan, but the total investment increase is calculated by energy-saving operation cost, and the investment can be recovered in 238 days.
It can be seen that the separation process provided in example 1 of the present invention has the following features and advantages:
(1) the process method provided by the embodiment of the utility model is used for separating the sulfuric acid process carbon four-alkylation reaction product to obtain the qualified isobutane product, normal butane product and alkylate oil product for circulation.
(2) By adopting the process method and the flow provided by the embodiment of the utility model, the isobutane product, the normal butane product and the alkylate oil product for circulation with the same index as that of the existing sulfuric acid alkylation process can be obtained.
(3) By adopting the new separation process provided by the embodiment of the utility model, qualified alkylate oil product is obtained from the bottom of the first rectifying tower T1, qualified isobutane for circulation is obtained from the top of the second rectifying tower T2, and qualified normal butane product is obtained from the bottom of the second rectifying tower T2.
(4) The new separation process provided by the embodiment of the utility model meets the use condition of heat pump rectification by adjusting the separation sequence.
(5) The new separation process provided by the embodiment of the utility model is additionally provided with a heat pump, the steam from the tower top is compressed and heated, enters a tower kettle reboiler of the second rectifying tower T2, is changed into a saturated liquid phase after heat exchange, is partially vaporized after being reduced in pressure and cooled, then enters a tower top condenser to be completely liquefied, and then part of the liquefied liquid enters the tower top of the second rectifying tower T2 as reflux liquid, and the other part of the liquefied liquid phase is extracted as a liquid phase product.
(6) The number of the trays of the first rectifying tower T1 is between 30 and 80, and the number of the trays of the second rectifying tower T2 is between 50 and 110. The first column is fed at a position in the lower middle of the column and the second column is fed at a position in the upper middle of the column.
(7) The novel separation process provided by the embodiment of the utility model has a very obvious energy-saving effect. The energy-saving effect can reach 28.09% based on the fraction part alone, and the energy consumption of the whole alkylation device can be reduced by more than 15%.
(8) The heat source of the auxiliary reboiler used in the novel separation process provided by the embodiment of the utility model can adopt low-pressure steam, and can also adopt condensed water or other low-temperature hot water, so that the quality of the heat source is reduced, and the operation cost is saved.
Compared with the prior art, the embodiment of the utility model has the following beneficial effects:
(1) the novel process can achieve the same separation effect as the prior art.
(2) The novel process of the utility model greatly saves energy consumption and operating cost.
(3) The investment cost increased by the novel process can be quickly recovered, and the practicability is very good.
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 (4)
1. A separation device of alkylation reaction products is characterized by comprising a first rectifying tower (T1), a first reboiler (H1), a first condenser (E1), a second rectifying tower (T2), a second reboiler (H2), a third reboiler (H3), a second condenser (E2), a vapor compressor (C1) and a regulating valve (V1); 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 outlet at the top of the first rectifying tower (T1) is connected with a feed inlet of a first condenser (E1) so as to enable the gas phase material to be completely condensed in the first condenser (E1), an outlet pipeline of the first condenser (E1) is divided into two parts, one part of condensate is connected to a liquid phase material reflux port at the top of the first rectifying tower (T1), the other part of condensate is connected to a raw material feed inlet of a second rectifying tower (T2), a gas phase material outlet at the top of the second rectifying tower (T2) is connected with an inlet of a steam compressor (C1), an outlet of the steam compressor (C1) is connected with a heat source inlet of a second reboiler (H2) at the bottom of the second rectifying tower (T2), a heat source outlet of a second reboiler (H2) is connected with an inlet of a regulating valve (V1), an outlet of the regulating valve (V1) is connected with an inlet of the second condenser (E2), and an outlet pipeline of the second condenser (E2) is divided into two parts, one path is taken as an isobutane discharging pipeline for circulation, and the other path is connected with a liquid phase material reflux port of a second rectifying tower (T2); 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; a liquid phase inlet of a third reboiler (H3) is connected with the tower kettle of the second rectifying tower (T2), and an outlet of the third reboiler (H3) 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 apparatus of claim 1, further comprising a fourth reboiler (H4), the fourth reboiler (H4) being located in the upper middle portion of the stripping section of the first rectification column (T1), the inlet of the fourth reboiler (H4) being used for conveying the liquid phase material in the first rectification column (T1) to the fourth reboiler (H4), and the outlet being used for conveying the vapor-liquid mixture material from the fourth reboiler (H4) back to the first rectification column (T1).
3. The separation device according to claim 1, wherein the first rectification column (T1) and the second rectification column (T2) are both conventional rectification columns; the number of trays of the first rectifying tower (T1) is 30-80, and the number of trays of the second rectifying tower (T2) is 50-110.
4. The separation apparatus according to claim 1, wherein the number of trays of the first rectification column (T1) is 50 to 60 and the number of trays of the second rectification column (T2) is 65 to 80.
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| CN202121992646.4U CN216062074U (en) | 2021-08-23 | 2021-08-23 | Separation device for alkylation reaction product |
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| CN202121992646.4U Active CN216062074U (en) | 2021-08-23 | 2021-08-23 | Separation device for alkylation reaction product |
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