CN115121000A - Energy-saving separation process and device for sulfuric acid alkylation reaction product - Google Patents
Energy-saving separation process and device for sulfuric acid alkylation reaction product Download PDFInfo
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- CN115121000A CN115121000A CN202210893131.1A CN202210893131A CN115121000A CN 115121000 A CN115121000 A CN 115121000A CN 202210893131 A CN202210893131 A CN 202210893131A CN 115121000 A CN115121000 A CN 115121000A
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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
- B01D3/141—Fractional distillation or use of a fractionation or rectification column where at least one distillation column contains at least one dividing wall
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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
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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
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
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Abstract
The invention discloses an energy-saving separation process and device for sulfuric acid alkylation reaction products, which comprise a lower partition plate rectifying tower, a steam compressor, an intermediate reboiler and the like. The separation process adopts the residual steam at the top of the tower as the heat source of a middle reboiler at the left side of the partition plate on the basis of the combined process of thermal coupling and heat pump, and further utilizes the condensation latent heat of the steam at the top of the tower. Under the condition of obtaining the same product index, compared with a thermal coupling and heat pump combined process, the energy consumption of the separation process is further reduced, compared with the existing process flow, the energy consumption and the operation cost of the whole separation process can be greatly reduced, and the method has a good industrial application prospect.
Description
Technical Field
The invention relates to the field of petrochemical industry, in particular to an energy-saving separation process and device 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 is the earliest and still widely used technique among various carbon tetra-alkylation techniques. Sulfuric acid used in the sulfuric acid alkylation technology is superior to hydrofluoric acid in safety, the problem of waste acid is properly solved, and the sulfuric acid alkylation technology enters the 21 st century, and with the acceleration of the upgrading of Chinese gasoline quality, the demand for high-octane gasoline blending components is rapidly increased, 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 with current sulfuric acid alkylation plants is the high energy consumption, wherein the energy consumption of the fractionation section is about 50% to 55% of the total energy consumption of the plant.
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 ℃, the energy consumption mainly comes from 1.0MPa steam consumed by the two tower reboilers, and the two fractionating towers consume about 24 tons of 1.0MPa steam per hour by taking a sulfuric acid alkylation device of 20 ten thousand tons/year as an example.
The separation process and the separation device (application number: 202110970436.3) of the alkylation reaction product of the Chinese patent adopt the combination of a thermal coupling technology and a heat pump rectification technology to realize the separation of the alkylation reaction product. The separation index same as that of the existing process is obtained, and meanwhile, the energy consumption of the whole separation process can be greatly reduced, and the operation cost of the device is greatly saved. In the patent, part of steam at the top of the clapboard tower is used as a reboiler heat source at the side II of the stripping section after being pressurized and heated, and part of steam is directly condensed, and the intermediate reboiler H3 heat source at the side I of the stripping section is preferably a low-temperature and cheap heat source such as heat medium water or condensed water.
Through further research, the energy consumption of the whole separation process can be further reduced. Accordingly, the present invention is particularly set forth.
Disclosure of Invention
The invention aims to provide an energy-saving separation process of a sulfuric acid alkylation reaction product, which aims to further reduce separation energy consumption and save operation cost while achieving a separation target.
An energy-saving separation process of sulfuric acid alkylation reaction products is characterized in that on the basis of a thermal coupling and heat pump combined process, part or all of redundant steam at the top of a tower is used as a heat source of a reboiler at the bottom of the right side of a partition plate of a rectifying tower and a reboiler in the middle of the left side of the partition plate of the rectifying tower, so that the utilization efficiency of the condensation latent heat of the steam at the top of the tower is improved;
the specific process flow comprises the following main steps: feeding an alkylation reaction product from the left side of a partition plate of a lower partition plate rectifying tower, obtaining a qualified alkylate oil product at the bottom of the tower on the left side of the partition plate, obtaining a qualified normal butane product at the bottom of the tower on the right side of the partition plate, and obtaining a qualified isobutane product for circulation at the top of the tower; ascending gas on two sides of the partition board converges in a public rectification area above the partition board, and reflux above the partition board is distributed on two sides of the partition board according to a certain proportion; pressurizing and heating partial or all steam extracted from the top of the partition plate rectifying tower by using a steam compressor, performing heat exchange to obtain liquid phase material flow by using the partial or all steam as a heat source of a tower bottom reboiler on the right side of the partition plate of the rectifying tower and an intermediate reboiler on the left side of the partition plate of the rectifying tower, and performing reduced pressure cooling; and taking out the excessive heat at the tower top by a condenser, refluxing one part of the condensate to the lower clapboard rectifying tower, and outputting the other part of the condensate as an isobutane product.
Preferably, a part of or all saturated steam output from the top of the lower clapboard rectifying tower is pressurized and heated by a steam compressor, the pressurized steam is preferentially used as a heat source of a reboiler at the bottom of the right side of the clapboard of the rectifying tower, and the redundant steam is used as a heat source of a middle reboiler at the left side of the clapboard.
Preferably, the number of the steam compressors is two; and pressurizing and heating partial or all saturated steam at the top of the lower clapboard rectifying tower by using two steam compressors respectively, wherein gas phases after pressurization and heating are respectively used as heat sources of a reboiler at the bottom of the right side of the clapboard and a reboiler at the middle of the right side of the clapboard.
Preferably, the middle reboiler at the left side of the partition is positioned at a proper position below the feed inlet at the left side of the partition of the lower partition rectifying tower; the number of the intermediate reboilers is 1-3. More preferably, the number of the intermediate reboilers is 1 to 2.
Preferably, the tower top temperature of the lower clapboard rectifying tower is 40-60 ℃, and the tower top pressure is 0.41-0.65 MPa; the temperature of the bottom of the tower on the left side of the clapboard of the lower clapboard rectifying tower is above 90 ℃, and the temperature of the bottom of the tower on the right side of the clapboard of the lower clapboard rectifying tower is 50-70 ℃.
The invention also claims an energy-saving separation device of the sulfuric acid alkylation reaction product, which comprises a lower clapboard rectifying tower (T1), a condenser (E1) and a liquid separation tank (V1); a vertical partition is arranged at the middle lower part in the lower partition rectifying tower (T1), and the interior of the partition rectifying tower (T1) is divided into three working sections, namely a partition section I, a partition section II and a common rectifying section III; the bottoms of the left and right sides of the clapboard of the lower clapboard rectifying tower (T1) are respectively provided with a first reboiler (H1) and a second reboiler (H2); a raw material feeding port is formed in the side I of the partition plate section, and a third reboiler (H3) is arranged below the feeding port; the bottom discharge port of the partition section I of the lower partition rectifying tower (T1) is connected with an alkylate oil discharge pipeline; the liquid phase inlet of the first reboiler (H1) is connected with the tower bottom of the partition section I of the lower partition rectifying tower (T1), and the outlet of the first reboiler (H1) is connected with the tower body of the partition section I of the lower partition rectifying tower (T1); the liquid phase inlet of the second reboiler (H2) is connected with the tower kettle of the partition section II through a pipeline, the outlet of the second reboiler (H2) is connected with the tower body of the partition section II, and the tower bottom discharge port of the partition section II is connected with a normal butane discharge pipeline; the overhead vapor output pipeline of the common rectifying section III of the lower partition plate rectifying tower (T1) is divided into two parts, one part is connected with the inlet of the condenser (E1), and the other part is connected with the gas phase inlet of the liquid separation tank (V1); an outlet pipeline of the condenser (E1) is divided into two parts, one part is connected to a reflux inlet at the top of the clapboard rectifying tower (T1), and the other part is used as a circulating isobutane discharging pipeline; the third reboiler (H3) having a feed inlet for feeding a liquid phase feed from the column to the left of the partition of the lower partition rectification column (T1) to the third reboiler (H3) and a discharge outlet for feeding a vapor-liquid mixture feed from the third reboiler (H3) back to the column to the left of the partition of the lower partition rectification column (T1); the third reboiler (H3) comprises 1-3 once-through reboilers, and the reboilers are located below the feed inlet on the left side of the partition plate and located at different positions respectively.
Preferably, the separation device further comprises a vapor compressor (C1) and a regulating valve (PV 1); a steam outlet at the top of the liquid separation tank (V1) is connected with an inlet of the steam compressor (C1), an outlet pipeline of the steam compressor (C1) is divided into two parts, one part is connected with a heat source inlet of a second reboiler (H2) at the bottom of the right side of the partition plate, and the other part is connected with a heat source inlet of a third reboiler (H3) below a feed inlet at the left side of the partition plate; the heat source outlets of the second reboiler (H2) and the third reboiler (H3) are connected with the inlet of the regulating valve (PV1), the outlet of the regulating valve (PV1) is connected with the gas-liquid mixing inlet of the liquid separation tank (V1), and the liquid phase outlet at the bottom of the liquid separation tank (V1) is connected with the top reflux inlet of the partition distillation column (T1).
As another preferable mode, the separation apparatus further comprises a vapor compressor (C1), a vapor compressor (C2), a regulating valve (PV1) and a regulating valve (PV 2); a steam outlet pipeline at the top of the liquid separation tank (V1) is divided into two parts, one part is connected with the inlet of a steam compressor (C1), and the other part is connected with the inlet of the steam compressor (C2); the outlet of the vapor compressor (C1) is connected with the heat source inlet of a second reboiler (H2) at the bottom of the right side of the clapboard, and the outlet of the vapor compressor (C2) is connected with the heat source inlet of a third reboiler (H3) below the feed inlet at the left side of the clapboard; the heat source outlets of the second reboiler (H2) and the third reboiler (H3) are respectively connected with a regulating valve (PV1) and a regulating valve (PV2), and then are respectively connected with the gas-liquid mixing inlet of the liquid separation tank (V1), and the liquid phase outlet at the bottom of the liquid separation tank (V1) is connected with the top reflux inlet of the partition rectifying tower (T1).
Preferably, the theoretical plate numbers of the partition section I and the partition section II of the partition rectifying tower (T1) are both 20-60, the theoretical plate number of the common rectifying section III is 8-30, and the plate numbers of the partition section I and the partition section II are the same or different; the baffle plate rectifying tower (T1) is a plate tower, a packed tower or any combination of the two.
The invention also claims that the energy-saving separation process is suitable for separating sulfuric acid alkylation reaction products and is also suitable for a separation process of separating three similar products from a mixture consisting of two light hydrocarbons with similar boiling points and heavy hydrocarbons.
Compared with the prior art, the invention has the beneficial effects that:
on the basis of the invention patent (application number: 202110970436.3), the latent heat of the gas phase at the top of the tower is more fully utilized, the energy consumption of the device is reduced, and the operation cost is saved. Compared with a thermal coupling and heat pump combined process, the energy consumption can be reduced by 10-20%; compared with the conventional two-tower direct sequence process of rectification used in the existing industry, the energy consumption can be reduced by 43.2-51%, and the energy consumption of the whole sulfuric acid alkylation device can be reduced by 21.6-28%.
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 process flow diagram in a comparative example of the present invention;
FIG. 2 is a first process flow diagram provided by the present invention;
FIG. 3 is a second process flow diagram provided by the present invention;
FIG. 4 is a flow chart of the process in the comparative example of the present invention.
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 invention. 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 invention, as claimed, but is merely representative of selected embodiments of the invention. 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 absolutely horizontal or hanging, but 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 invention provides an energy-saving separation device for 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 invention can be adopted, and the separation device comprises a partition rectification tower T1, a condenser E1, a liquid separation tank V1, a first reboiler H1, a second reboiler H2, a third reboiler H3, a vapor compressor C1 and a regulating valve PV 1.
A raw material feeding hole is formed in the side of the partition plate section I, and a bottom discharge hole of the partition plate section I of the partition plate rectifying tower T1 is connected with an alkylate oil discharge pipeline; the liquid phase inlet of the first reboiler H1 is connected with the tower kettle of the partition section I of the partition rectifying tower T1, and the outlet of the first reboiler H1 is connected with the tower body of the partition section I of the partition rectifying tower T1; the liquid phase inlet of the second reboiler H2 is connected with the tower kettle of the partition section II through a pipeline, the outlet of the second reboiler H2 is connected with the tower body of the partition section II, and the discharge hole at the bottom of the tower of the partition section II is connected with a normal butane discharge pipeline. A tower top steam output pipeline of a public rectifying section III of the clapboard rectifying tower T1 is divided into two parts, one part is connected with an inlet of a condenser E1, and the other part is connected with a gas phase inlet of a liquid separating tank V1; an outlet pipeline of the condenser E1 is divided into two parts, one part is connected to a reflux liquid inlet at the top of the clapboard rectifying tower T1, and the other part is used as a discharge pipeline of the isobutane for circulation. The third reboiler H3 is a one-pass reboiler and is located below the feed inlet of the partition section I of the partition rectifying tower T1, the third reboiler H3 is provided with a feed inlet and a discharge outlet, the feed inlet is used for conveying materials from the tower on the left side of the partition rectifying tower T1 to the third reboiler H3, and the discharge outlet is used for conveying vapor-liquid mixed materials from the third reboiler H3 back to the tower on the left side of the partition rectifying tower T1.
A steam outlet at the top of the liquid separation tank V1 is connected with an inlet of the steam compressor C1, an outlet pipeline of the steam compressor C1 is divided into two parts, one part is connected with a heat source inlet of a second reboiler H2 at the bottom of the right side of the partition plate, and the other part is connected with a heat source inlet of a third reboiler H3 below a feed inlet at the left side of the partition plate; the heat source outlets of the second reboiler H2 and the third reboiler H3 are connected with the inlet of an adjusting valve PV1, the outlet of the adjusting valve PV1 is connected with the gas-liquid mixing inlet of a liquid separating tank V1, and the liquid phase outlet at the bottom of the liquid separating tank V1 is connected with the top reflux inlet of a partition rectifying tower T1.
In specific implementation, the baffle rectification column T1 can be a plate column, a packed column, or any combination of the two. The theoretical plate numbers of the partition section I and the partition section II of the partition rectifying tower T1 are both 20-60, the theoretical plate number of the common rectifying section III is 8-30, and the plate numbers of the partition section I and the partition section II can be the same or different. The partition plate in the partition plate rectifying tower T1 can be arranged in the center or eccentrically and is determined by calculation according to the composition of the raw materials and the separation index.
In specific implementation, the condenser E1 is a condenser using air or cooling water as a condensing medium. When cooling water is used as a cooling medium, the temperature at the top of the tower is 40-60 ℃, the pressure at the top of the tower is 0.42-0.6MPa (g), the temperature at the bottom of the tower at the left side of the clapboard is higher than 90 ℃, and the temperature at the bottom of the tower at the right side of the clapboard is 50-70 ℃. The pressure of the tower kettle on the left side of the clapboard and the pressure of the tower kettle on the right side of the clapboard can be the same or different.
In specific implementation, the first reboiler H1 is a circulating reboiler using high-grade heat sources such as low-pressure steam or heat transfer oil.
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.
Examples
In the embodiment, the energy-saving separation device provided by the invention is used for separation, and the process flow shown in figure 2 is adopted.
The sulfuric acid alkylation reaction product raw material is fed from the appropriate 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 reaches the standard by adopting a proper tower structure and optimizing operation conditions. The calculation results are as follows:
the heating amount of the first reboiler H1 was 3945.18kw, the power consumption of the compressor C1 was 1039.05kw, the reduced heat energy consumption was 2597.63kw, the power consumption of the compressor C2 was 596.09kw, and the reduced heat energy was 1490.23 kw. The total heat load was 8033.04 kw.
The energy consumption of the condenser E1 was-4030.64 kw, i.e. a total cooling load of-4030.64 kw.
Comparative example 1
The process flow in fig. 4 is used.
The sulfuric acid alkylation reaction product raw material is fed from the appropriate 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 reaches the standard by adopting a proper tower structure and optimizing operation conditions. The calculation results are as follows:
the calculation results are as follows: the heating amount of the first reboiler H1 was 6944.22kw, the power consumption of the compressor C1 was 1020.39kw, the reduced energy consumption of thermal energy was 2550.98kw, and the total thermal load was 9495.2 kw. The energy consumption of the condenser E1 was-6445.99 kw, i.e. a total cooling load of-6445.99 kw.
A comparison of comparative example 1 and the examples is shown in table 2:
TABLE 2 comparison of energy consumption for comparative example 1 and example 1
| Contrast item | Comparative example 1 | Examples | Energy saving value | Energy saving ratio |
| Heat load (kw) | 9495.2 | 8033.04 | 1462.16 | 15.40％ |
| Cold load (kw) | -6445.99 | -4030.64 | -2415.35 | 37.47％ |
Comparative example 2
With the existing process flow, the whole process comprises two conventional rectifying towers as shown in figure 1.
The sulfuric acid alkylation reaction product raw material is fed from the appropriate 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 reaches the standard by adopting a proper tower structure and optimizing operation conditions. The calculation results are as follows:
the heating amount of the bottom of the rectifying tower T1 is 12819.92kw, the heating amount of the bottom of the rectifying tower T2 is 2131.46kw, and the total heat load is 14951.38 kw. The energy consumption of the overhead condenser of the rectifying tower T1 is-12369.57 kw, the energy consumption of the overhead condenser of the rectifying tower T2 is-1703.92 kw, and the total cooling load is-14073.49 kw.
The comparative example 2 and the comparative example 1 are shown in table 3:
TABLE 3 comparison of energy consumption of comparative example 2 and example 1
| Contrast item | Comparative example 2 | Examples | Energy saving value | Energy saving ratio |
| Heat load (kw) | 14951.38 | 8033.04 | 6918.34 | 46.27％ |
| Cold load (kw) | -14073.49 | -4030.64 | -10042.85 | 71.36％ |
It can be seen from a comparison of tables 2 and 3 that the separation process provides further savings in energy consumption and operating costs compared to the use of a thermal coupling alone in combination with a heat pump process. Compared with the conventional two-tower direct sequence flow of rectification in the prior industrial application, the method has great energy-saving effect.
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 (10)
1. An energy-saving separation process of sulfuric acid alkylation reaction products is characterized in that on the basis of a thermal coupling and heat pump combined process, partial or all redundant steam at the top of a tower is used as a heat source of a reboiler at the bottom of the tower at the right side of a partition plate of a lower partition plate rectifying tower and a reboiler in the middle of the left side of the partition plate of the rectifying tower, so that the utilization efficiency of the latent heat of condensation of the steam at the top of the tower is improved;
the specific process flow comprises the following main steps: feeding an alkylation reaction product from the left side of a partition plate of a lower partition plate rectifying tower, obtaining a qualified alkylate oil product at the bottom of the tower on the left side of the partition plate, obtaining a qualified normal butane product at the bottom of the tower on the right side of the partition plate, and obtaining a qualified isobutane product for circulation at the top of the tower; ascending gas on two sides of the partition board converges in a public rectification area above the partition board, and reflux liquid above the partition board is distributed on two sides of the partition board according to a certain proportion; pressurizing and heating partial or all steam extracted from the top of the partition plate rectifying tower by using a steam compressor, performing heat exchange to obtain liquid phase material flow by using the partial or all steam as a heat source of a tower bottom reboiler on the right side of the partition plate of the rectifying tower and an intermediate reboiler on the left side of the partition plate of the rectifying tower, and performing reduced pressure cooling; and taking out the surplus heat at the tower top by a condenser, refluxing one part of the condensate to return to the lower clapboard rectifying tower, and outputting the other part of the condensate as an isobutane product.
2. The energy-saving separation process of claim 1, wherein part or all of the saturated steam output from the top of the lower clapboard rectifying tower is pressurized and heated by a steam compressor, and is preferentially used as a heat source of a reboiler at the bottom of the right side of the clapboard of the rectifying tower, and the surplus part is used as a heat source of a reboiler at the middle of the left side of the clapboard.
3. The energy efficient separation process of claim 1 or 2 wherein there are two vapor compressors; and pressurizing and heating partial or all saturated steam at the top of the lower clapboard rectifying tower by using two steam compressors respectively, wherein gas phases after pressurization and heating are respectively used as heat sources of a reboiler at the bottom of the right side of the clapboard and a reboiler at the middle of the right side of the clapboard.
4. The energy-saving separation process of claim 1, wherein the middle reboiler at the left side of the partition is positioned at a proper position below the feed inlet at the left side of the partition of the lower partition rectification column; the number of the intermediate reboilers is 1-3.
5. The energy-saving separation process of claim 1, wherein the top temperature of the lower baffle distillation column is 40-60 ℃, and the top pressure is 0.41-0.65 MPa; the temperature of the tower bottom on the left side of the clapboard of the lower clapboard rectifying tower is above 90 ℃, and the temperature of the tower bottom on the right side of the clapboard of the lower clapboard rectifying tower is 50-70 ℃.
6. An energy-saving separation device for sulfuric acid alkylation reaction products is characterized by comprising a lower partition plate rectifying tower (T1), a condenser (E1) and a liquid separation tank (V1); a vertical partition is arranged at the middle lower part in the lower partition rectifying tower (T1), and the interior of the partition rectifying tower (T1) is divided into three working sections, namely a partition section I, a partition section II and a common rectifying section III; the bottoms of the left and right sides of the partition plate of the lower partition plate rectifying tower (T1) are respectively provided with a first reboiler (H1) and a second reboiler (H2); a raw material feeding hole is formed in the side I of the partition plate section, and a third reboiler (H3) is arranged below the feeding hole; the bottom discharge port of the partition section I of the lower partition rectifying tower (T1) is connected with an alkylate oil discharge pipeline; the liquid phase inlet of the first reboiler (H1) is connected with the tower bottom of the partition section I of the lower partition rectifying tower (T1), and the outlet of the first reboiler (H1) is connected with the tower body of the partition section I of the lower partition rectifying tower (T1); the liquid phase inlet of the second reboiler (H2) is connected with the tower kettle of the partition section II through a pipeline, the outlet of the second reboiler (H2) is connected with the tower body of the partition section II, and the tower bottom discharge port of the partition section II is connected with a normal butane discharge pipeline; the overhead vapor output pipeline of the common rectifying section III of the lower partition plate rectifying tower (T1) is divided into two parts, one part is connected with the inlet of the condenser (E1), and the other part is connected with the gas phase inlet of the liquid separation tank (V1); an outlet pipeline of the condenser (E1) is divided into two parts, one part is connected to a reflux inlet at the top of the clapboard rectifying tower (T1), and the other part is used as an isobutane discharging pipeline for circulation; the third reboiler (H3) having a feed inlet for feeding a liquid phase feed from the column to the left of the partition of the lower partition rectification column (T1) to the third reboiler (H3) and a discharge outlet for feeding a vapor-liquid mixture feed from the third reboiler (H3) back to the column to the left of the partition of the lower partition rectification column (T1); the third reboiler (H3) comprises 1-3 once-through reboilers, and the reboilers are located below the feed inlet on the left side of the partition plate and located at different positions respectively.
7. The separation device according to claim 6, further comprising a vapor compressor (C1) and a regulating valve (PV 1); a steam outlet at the top of the liquid separation tank (V1) is connected with an inlet of the steam compressor (C1), an outlet pipeline of the steam compressor (C1) is divided into two parts, one part is connected with a heat source inlet of a second reboiler (H2) at the bottom of the right side of the partition plate, and the other part is connected with a heat source inlet of a third reboiler (H3) below a feed inlet at the left side of the partition plate; the heat source outlets of the second reboiler (H2) and the third reboiler (H3) are connected with the inlet of the regulating valve (PV1), the outlet of the regulating valve (PV1) is connected with the gas-liquid mixing inlet of the liquid separation tank (V1), and the liquid phase outlet at the bottom of the liquid separation tank (V1) is connected with the top reflux inlet of the partition distillation column (T1).
8. The separation device of claim 6, further comprising a vapor compressor (C1), a vapor compressor (C2), a regulating valve (PV1), and a regulating valve (PV 2); a steam outlet pipeline at the top of the liquid separation tank (V1) is divided into two parts, one part is connected with the inlet of a steam compressor (C1), and the other part is connected with the inlet of the steam compressor (C2); the outlet of the vapor compressor (C1) is connected with the heat source inlet of a second reboiler (H2) at the bottom of the right side of the clapboard, and the outlet of the vapor compressor (C2) is connected with the heat source inlet of a third reboiler (H3) below the feed inlet at the left side of the clapboard; the heat source outlets of the second reboiler (H2) and the third reboiler (H3) are respectively connected with a regulating valve (PV1) and a regulating valve (PV2), and then are respectively connected with the gas-liquid mixing inlet of the liquid separation tank (V1), and the liquid phase outlet at the bottom of the liquid separation tank (V1) is connected with the top reflux inlet of the partition rectifying tower (T1).
9. The separation apparatus according to claim 6, wherein the number of theoretical plates of the partition section I and the partition section II of the partition rectifying column (T1) is 20 to 60, the number of theoretical plates of the common rectifying section III is 8 to 30, and the number of plates of the partition section I and the partition section II is the same or different; the baffle plate rectifying tower (T1) is a plate tower, a packed tower or any combination of the two.
10. The energy-saving separation process of claim 1 is suitable for separation of sulfuric acid alkylation reaction products, and is also suitable for separation of three similar products obtained by separation of a mixture consisting of two light hydrocarbons with similar boiling points and heavy hydrocarbons.
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