CN112791435A - Thermal coupling rectification device and thermal coupling rectification process - Google Patents
Thermal coupling rectification device and thermal coupling rectification process Download PDFInfo
- Publication number
- CN112791435A CN112791435A CN201911104596.9A CN201911104596A CN112791435A CN 112791435 A CN112791435 A CN 112791435A CN 201911104596 A CN201911104596 A CN 201911104596A CN 112791435 A CN112791435 A CN 112791435A
- Authority
- CN
- China
- Prior art keywords
- tower
- rectification
- subsequent
- rectifying tower
- stripping
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- 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
-
- 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
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/38—Steam distillation
-
- C—CHEMISTRY; METALLURGY
- 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
- C10G7/00—Distillation of hydrocarbon oils
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a thermal coupling rectification device, which comprises a preorder rectification tower T101 and a subsequent rectification tower T102 which are connected in series, wherein 1 or more than 1 lateral line coupling material flow pipeline for connecting the preorder rectification tower T101 and the subsequent rectification tower T102 is also arranged above a tower bottom discharge hole of the preorder rectification tower T101 and a tower bottom feed inlet of the subsequent rectification tower T102; more than 1 complete thermal coupling stripping tower is arranged on one side of the subsequent rectifying tower T102. The invention also provides a rectification process based on the thermally coupled rectification device and application thereof. Compared with the conventional rectifying device, the thermal coupling rectifying device provided by the invention has less equipment investment; the rectification process method based on the rectification device can reduce energy consumption, improve product quality and has obvious economic benefit.
Description
Technical Field
The invention belongs to the field of petroleum product processing, and particularly relates to a thermal coupling rectification device and a thermal coupling rectification process based on the same.
Technical Field
The rectification unit is an important ring in the petroleum processing process, and the separation effect directly influences the quality of a final product. Conventional separation of multi-component mixtures employs a series of simple rectification columns in series, each column having a distinct separation task. FIG. 1 shows a flow chart of product separation in a conventional base oil hydrogenation process involving two rectification columns T1 and T2 connected in series, wherein the product to be separated is heated by a heating furnace and then enters the preceding rectification column T1, and the bottom product of the preceding rectification column is heated by a reboiler or a heating furnace and then enters the subsequent rectification column T2. That is, each column has a condenser and a heating device. Such a process makes rectification a highly energy-consuming process. According to statistics, the energy consumption of rectification accounts for more than 60% of the total energy consumption in the petrochemical industry.
If one liquid phase material flow is led out from one tower and directly used as the tower top liquid phase reflux of the other tower or one gas phase material flow is led out from one tower and directly used as the tower bottom gas phase reflux of the other tower, condensers or heating equipment can be avoided in some towers, and direct heat coupling is realized, so that the aim of saving energy is fulfilled. The rectification containing the structure is the thermocouple rectification.
Chinese invention patent application publication No. CN102641604A (publication No. 2012, 8, 22) discloses a process of multi-component side line thermal coupling rectification: a side line connection is added outside the original connection between the two rectifying towers, the mixture extracted from the side line of the first rectifying tower is used as the newly added feed stream of the second rectifying tower, and the feeding position of the mixture is positioned above the original feeding position. The process flow is shown in figure 2. The side line thermal coupling rectification can achieve about 10 percent of energy-saving effect.
Different from a common rectifying tower, the material to be separated in the petrochemical industry is crude oil or secondary processing oil (including fractions such as fuel oil, lubricating oil base oil and the like) with complex components, the secondary processing oil enters the rectifying tower after being heated and vaporized, gas-liquid exchange is carried out on tower plates or fillers, and finally different products are obtained at the tower top, the tower bottom and the lateral line. In order to balance the gas-liquid load in the tower and ensure the heat balance of the whole tower, a plurality of middle-section reflux streams are generally required to be arranged; three mid-stream reflux streams 1, 2 and 3 as set up in the subsequent rectification column T2 in fig. 1. Besides, in order to meet the quality requirement of the side product, a side product stripping tower is required to be arranged outside the main tower to remove light components in the product; three stripping columns 4, 5 and 6 are provided as in the subsequent rectification column T2 in fig. 1. The stripping column requires continuous steam to be supplied externally, further increasing the energy consumption of the rectification process.
Therefore, there is a need to improve and develop a thermal coupling rectification process with better energy-saving effect, and meet the requirements of energy conservation, consumption reduction and emission reduction in the petrochemical industry.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a novel thermally coupled rectification device and a rectification process based on the device. Compared with the traditional device, the thermal coupling rectification device can reduce the investment of the tower body equipment of the rectification tower and has obvious cost advantage. On the premise of not influencing the product quality, the rectification process has obvious energy-saving effect. The rectification process can also be used for the reconstruction of the existing device, and has remarkable practicability and wide application prospect.
In order to achieve the purpose of the invention, the invention adopts the following technical scheme:
a thermal coupling rectification device comprises a preorder rectification tower T101 and a subsequent rectification tower T102 which are connected in series, wherein a series pipeline is connected with a tower bottom discharge hole of the preorder rectification tower T101 and a tower bottom feed inlet of the subsequent rectification tower T102, and a heating furnace is arranged on the series pipeline in front of the tower bottom feed inlet of the subsequent rectification tower T102; 1 or more than 1 lateral line coupled material flow pipelines which are connected with the preorder rectifying tower T101 and the subsequent rectifying tower T102 are also arranged above the tower bottom discharge hole of the preorder rectifying tower T101 and the tower bottom feed inlet of the subsequent rectifying tower T102; more than 1 complete thermal coupling stripping tower is arranged on one side of the subsequent rectifying tower T102, and more than 1 reflux device is arranged on the other side; the complete thermal coupling stripping tower is provided with 2 pipelines at the top and the bottom respectively to be connected with the subsequent rectifying tower T102, and the middle part is provided with a lateral line product extraction pipeline.
Preferably, 1 side-coupled material flow pipeline is arranged between the preceding rectifying tower T101 and the subsequent rectifying tower T102.
Preferably, the subsequent rectification column T102 is connected to the side-coupled stream line at a position not lower than the middle portion.
Preferably, the subsequent rectification column T102 is provided with 1 overhead reflux, 1 or more mid-stream reflux.
As a preferred embodiment, the subsequent rectification column T102 is sequentially provided with 1 overhead reflux and 2 middle reflux from top to bottom.
Preferably, the overhead reflux stream is withdrawn from 1 to 2 trays below the top of the subsequent rectification column T102, and the stream is returned to the column at tray 1 of the subsequent rectification column T102.
The subsequent rectification column T102 may comprise 2 or 3 strippers, depending on the number of products to be separated; the top of the stripping tower is connected with the subsequent rectifying tower T102 through two pipelines, and the bottom of the stripping tower is provided with a steam inlet pipeline and a side product output pipeline.
Preferably, the bottom of the subsequent rectification column T102 is also provided with a steam inlet line.
Preferably, the subsequent rectifying tower T102 is provided with a water or non-condensable vapor extraction line at the top of the tower.
Preferably, the subsequent rectifying tower T102 is provided with a side product output pipeline at the 1 st to 2 nd tower plates.
In the specification, the tower plate is a theoretical plate and is counted from top to bottom of the rectifying tower.
The invention also aims to provide a rectification process based on the thermally coupled rectification device, and the specific process flow comprises the following steps:
(1) separation in a preceding rectification column T101
The material to be separated enters the preorder rectifying tower T101 after being heated, light fraction is obtained from the top of the preorder rectifying tower T101, a side-draw material flow of the preorder rectifying tower T101 directly enters the subsequent rectifying tower T102 through a side-coupled material flow pipeline without being heated, and a bottom material of the preorder rectifying tower T101 flows through the series pipeline and is heated by the heating furnace and then enters the subsequent rectifying tower T102;
(2) superheated steam enters the bottom of the subsequent rectifying tower T102 and the bottom of the stripping tower through the steam inlet pipeline respectively to provide heat for the vaporization of a stream in the tower;
(3) separation in the subsequent rectification column T102
Heating the bottom material flow of the preorder rectifying tower T101, then carrying out steam stripping on the bottom material flow in the subsequent rectifying tower T102, taking unvaporized liquid phase as heavy fraction to be extracted from the bottom of the T102, enabling a gas phase material flow to ascend from a lower tower plate, continuously carrying out gas-liquid exchange with the liquid phase below an upper tower plate, recovering the heat in the tower through middle-section reflux and tower top reflux, simultaneously enabling part of the gas phase material flow to enter the complete thermal coupling stripping tower and the stripping tower for steam stripping, and finally respectively obtaining different side line products from the position close to the top of the subsequent rectifying tower, the middle part of the complete thermal coupling stripping tower and the bottom of the stripping; and water or non-condensable vapor is produced at the top of the subsequent rectifying tower.
Preferably, the preceding rectifying column T101 and the subsequent rectifying column T102 are atmospheric columns or vacuum columns.
The theoretical plate number of the preorder rectifying tower T101 is determined according to the material to be separated and the separation precision requirement.
Preferably, the theoretical plate number of the preorder rectifying tower T101 is more than or equal to 5; more preferably, the number of theoretical plates of the preceding rectifying column T101 is 5-10.
The theoretical plate number of the subsequent rectifying tower T102 is determined according to the number of the side line products, and 5-7 plates are required to be arranged between two adjacent side line products. Therefore, the theoretical plate number of the subsequent rectifying tower T102 is preferably equal to or more than 15, and more preferably, the theoretical plate number of the subsequent rectifying tower T102 is 24-28 when 4 side products and 1 tower bottom heavy fraction are obtained simultaneously.
Preferably, the theoretical plate number of the complete thermal coupling stripping tower or the stripping tower is 4-6.
Preferably, the outlet temperature of the heating furnace is less than or equal to 390 ℃.
Preferably, the flow rate of the coupled gas-phase material flow between the subsequent rectifying tower T102 and the complete thermal coupling stripping tower is less than or equal to 1100kg/h, more preferably 900-1100 kg/h, and the flow rate of the coupled liquid-phase material flow is about 24100-2450 kg/h.
Preferably, the flow rate of the top reflux of the subsequent rectifying tower T102 is 30000-45000 kg/h, the flow rate of the first middle section reflux is 10000-20000 kg/h, and the flow rate of the second middle section reflux is 20000-30000 kg/h from top to bottom.
The invention also aims to provide the application of the rectification process in the atmospheric and vacuum distillation of crude oil and the cutting of secondary processing oil products.
Specifically, the cutting of the secondary processed oil product comprises the cutting of a catalytic cracking product into gasoline and diesel oil, and the cutting of the oil product subjected to the hydrotreatment into the gasoline, the diesel oil and various grades of hydrogenated base oil.
The thermal coupling rectifying device provided by the invention is characterized in that at least 1 side line material flow pipeline is arranged between the original preorder rectifying tower and the subsequent rectifying tower, so that partial thermal coupling between the two rectifying towers is realized. The subsequent rectification column and the at least 1 side stripper are in completely thermally coupled form, the bottom of which no longer uses steam or other heating methods.
Based on the rectification process of the thermally coupled rectification device, the energy conservation and the consumption reduction are realized through the following ways;
in the conventional two-tower separation process of petroleum products, tower bottom material flow of a preorder rectifying tower completely enters a heating furnace, and enters a subsequent rectifying tower for further separation after being vaporized for one time. The energy consumption of the furnace is proportional to the flow rate of the stream to be heated entering the furnace. According to the invention, a liquid phase material flow is extracted from the middle section of the preceding rectifying tower, and the existence of the material flow reduces the flow of the material flow to be heated entering the heating furnace, so that the energy consumption of the heating furnace is greatly reduced, and the flow consumption reduction is realized.
The gas phase in the subsequent rectifying tower mainly comes from the gas phase stream after primary gasification in the heating furnace, and the liquid phase stream entering the heating furnace is reduced due to the existence of the side line coupling stream, so that the gas phase stream in the tower is directly reduced. The diameter of the rectifying tower is closely related to the flow of the gas-phase material flow in the tower, the gas-phase material flow in the tower is reduced, and the diameter of the rectifying tower can be correspondingly reduced. For the design of the new device, the investment cost of the tower body cost of the subsequent rectifying tower can be directly reduced.
The subsequent rectification column and the at least 1 side stripper of the present invention are connected in a fully thermally coupled manner. At the moment, the bottom of the stripping tower does not need to additionally introduce stripping steam, and other heating equipment is not needed; the heat input required for this comes entirely from the gas phase stream in the subsequent rectification column entering from the bottom of the fully thermally coupled stripper column. On the premise of ensuring the separation requirement of the product, the use of stripping steam is reduced, and the effects of energy conservation and consumption reduction are achieved. In addition, the reduction of the use amount of the stripping steam also reduces the water content in the side product, and improves the product quality.
Drawings
The present invention will be described in detail with reference to the accompanying drawings.
Fig. 1 shows a schematic structure of a prior art series rectification device. Wherein:
t1-preceding rectifying column; t2 — subsequent rectification column; 1. 2 and 3-middle section reflux; 4. 5 and 6-stripper.
Fig. 2 shows a schematic diagram of a typical side-coupled enhanced distillation device.
Fig. 3 is a schematic structural view of the thermally coupled rectification apparatus of embodiment 1. Wherein:
t101-preceding rectifying column; t102-a subsequent rectification column; 1-series line between T101 and T102; 2-heating the furnace; 3-a side-coupled material flow pipeline; 4-overhead reflux; 5-refluxing the first middle section; 6-second middle section reflux; 7-side stripper 1; 8-side stripper 2; 9-a fully thermally coupled stripper column; 10-steam inlet line; 11-water or non-condensing steam extraction line; a 12-T102 sidedraw product outlet line; 13-a side product output pipeline of the side stripper 1; 14-side product output pipeline of side stripper 2; 15-a fully thermally coupled stripper sidedraw product output line; a 16-T102 bottom heavy fraction output line; 17-T101 overhead light fraction output pipeline.
Detailed Description
The present invention will be described in detail below with reference to specific embodiments.
The specific implementation can be determined according to the actual requirements of different refineries. If the construction of a new plant is involved, the thermally coupled rectification plant of the present invention can be employed in its entirety at the initial stage of the design. If only the existing device is modified, the existing device can be modified into the thermally coupled rectification device of the invention by replacing and adding tower parts on the basis of comprehensively considering the modification feasibility. The present invention will be described in detail with reference to the drawings, but the present invention is not limited thereto.
In the following examples, the "95% true boiling point distillation temperature" refers to the temperature required for distilling an oil product by using a true boiling point distillation method to distill 95% of the oil product by mass.
Example 1A thermally coupled rectification apparatus
A structural schematic diagram of a thermally coupled rectification device is shown in figure 3, and the thermally coupled rectification device comprises a preorder rectification tower T101 and a follow-up rectification tower T102 which are connected in series, wherein a series pipeline 1 is connected with a tower bottom discharge hole of the preorder rectification tower T101 and a tower bottom feed inlet of the follow-up rectification tower T102, and a heating furnace 2 is arranged in front of the tower bottom feed inlet of the follow-up rectification tower T102 on the series pipeline 1. 1 side line coupling material flow pipeline 3 is arranged between the bottom discharge hole of the preceding rectifying tower T101 and the middle part of the subsequent rectifying tower T102.
One side of the subsequent rectifying tower T102 is provided with 1 complete thermal coupling stripping tower 9, the top and the bottom of the complete thermal coupling stripping tower 9 are respectively provided with 2 complete thermal coupling material flow pipelines 17 connected with the subsequent rectifying tower T102, and the middle part of the complete thermal coupling stripping tower is provided with a side product extraction pipeline 15. The subsequent rectifying tower T102 is arranged at the same side of the completely thermally coupled stripping tower 9 and is also provided with stripping towers 7 and 8, the top of the side stripping towers 7 and 8 is connected with the subsequent rectifying tower T102 through two pipelines, and the bottoms of the side stripping towers 7 and 8 are provided with a steam inlet pipeline 10 and side product output pipelines 13 and 14. And 1 tower top reflux 4, a first middle section reflux 5 and a second middle section reflux 6 are sequentially arranged on the other side of the subsequent rectifying tower T102 from top to bottom. And the tower top reflux 4 is used for extracting material flow from 1-2 tower plates below the tower top of the subsequent rectifying tower T102, and the material flow is returned to the tower from the 1 st tower plate of the subsequent rectifying tower T102.
The top of the preorder rectifying tower T101 is provided with a light fraction output pipeline 17.
The bottom of the subsequent rectifying tower T102 is also provided with a steam inlet pipeline 10 and a tower bottom heavy fraction output pipeline; the top of the T102 is provided with a water or noncondensable steam extraction pipeline 11. T102 is provided with a side product output pipeline 12 at the 1 st to 2 nd tower plates.
EXAMPLE 2 rectification of hydrogenated base oils
The rectification in this example is based on the thermally coupled rectification apparatus described in example 1.
The true boiling point of the hydrogenated base oil is shown in Table 1, and the cutting scheme is obtained by analyzing the properties of the narrow cut. The cut points (95% true boiling temperature) for the light ends and the side streams were 350 deg.C, 390 deg.C, 410 deg.C, 450 deg.C and 500 deg.C, respectively.
T101 and T102 are vacuum towers, and the hydrogenated base oil is fed from the middle part of T101 after heat exchange is carried out to 200 ℃. A full condenser is adopted at the top of the T101 tower, and light fractions can be obtained at the top of the tower after separation and are output through a light fraction output pipeline 17; the side stream of T101 is extracted from the position of one tower plate above the tower bottom and directly enters T102 in the middle of T102 through a side coupling stream pipeline 3; the T101 bottom stream is passed through the series line 1 and heated to 334 ℃ by the furnace 2 and then enters T102 from a position above the third tray on the bottom of T102. Superheated steam enters T102 and stripping columns 7 and 8, respectively, via respective bottoms steam lines 10.
The liquid phase remaining after the bottom steam stripping of the stream once vaporized in the heating furnace 2 in T102 is withdrawn as a heavy fraction from the bottom of T102 via a heavy fraction outlet line 16. The stripped gas phase flows upwards in the T102, gas-liquid exchange is carried out between the gas phase and the liquid phase flowing down from the tower plate at the upper layer of the tower, and heat in the T102 tower is recovered through the first middle-stage reflux 5, the second middle-stage reflux 6 and the tower top reflux 4. A side product I is obtained at a position close to the top of the T102 and is output through a side product output pipeline 12, a side product II is obtained after the steam stripping of the bottom of the side stripping tower 7, the side product II is output through a side product output pipeline 13, and a side product III is obtained after the steam stripping of the bottom of the side stripping tower 8 and is output through a side product output pipeline 14. Two groups of connecting pipelines are arranged between the complete thermal coupling stripping tower 9 and the T102, the gas-liquid coupling material flows between the T102 and the complete thermal coupling stripping tower 9, a side product IV is obtained from the middle part of the complete thermal coupling stripping tower 9 and is output through a side product output pipeline 15.
Water or uncondensed steam is produced from the top of the T102 through a water or uncondensed steam production pipeline.
The main operating parameters of this example are shown in Table 2, and the actual boiling points of the respective products obtained by separation are shown in Table 3.
For comparison, the above-mentioned hydrogenated base oil was cut and separated on a conventional two-column series-connected rectification apparatus (schematic structure shown in fig. 1), and the main operation parameters thereof are shown in table 4, and the properties of each product are shown in table 5.
TABLE 1 true boiling point boiling range of hydrogenated base oils
| Mass fraction/%) | Temperature/. degree.C | Mass fraction/%) | Temperature/. degree.C |
| IBPa | 186 | 60.34 | 430 |
| 6.07 | 300 | 72.79 | 450 |
| 14.51 | 350 | 82.69 | 470 |
| 23.1 | 370 | 93.26 | 500 |
| 37.19 | 390 | 98.03 | 520 |
| 48.9 | 410 | EBPb | 540 |
aIBP (initial building point): initial boiling point, temperature at which the first gas phase is formed during the heating of the oil;
bEBP (end framing point): at the end point, the oil is heated to a temperature at which all the liquid is vaporized.
TABLE 2 Main operating parameters of the fully thermally coupled rectification Process of this example
*: the positions refer to trays within the corresponding T101 or T102.
TABLE 3 true boiling point of each product
TABLE 4 Main operating parameters of conventional rectification
*: the positions refer to the corresponding trays within T2.
TABLE 5 true boiling point distillation range of each product obtained by conventional rectification
Table 6 and Table 7 show the equipment investment and energy consumption of the thermally coupled rectification apparatus and the rectification process based on the thermally coupled rectification apparatus and the conventional two-tower rectification apparatus and separation process, respectively.
TABLE 6 thermal coupling rectification plant and rectification process equipment investment and energy consumption of the present invention
TABLE 7 Equipment investment and energy consumption of conventional two-column rectification apparatus and separation Process
The total load of the thermal coupling rectification process flow is 6.03MW, the tower diameter of the preorder rectification tower T101 is 3.44m, the tower diameter of the subsequent rectification tower T102 is 4.72m, and the total equipment investment is
The load of the conventional two-tower separation process in the prior art is 7.60MW, the tower diameter of a preceding rectifying tower T101 is 3.44m, the tower diameter of a subsequent rectifying tower T102 is 5.22m, and the equipment investment is
The data calculation shows that the process method provided by the invention can save 20.66% of energy and save about 2.0% of equipment investment compared with the conventional two-tower separation process.
The thermal coupling rectifying device and the rectifying process method based on the rectifying device have extremely remarkable economic benefit. The person skilled in the pertinent art can be fully adapted or adapted and combined with the method according to the invention for the separation of oil products and multicomponent mixtures. It is expressly stated that all such modifications or alterations and subcombinations which would be apparent to persons skilled in the art by making similar changes or variations to the process flow provided by the present invention are deemed to be within the spirit, scope and content of the invention.
Claims (10)
1. A thermal coupling rectification device comprises a preorder rectification tower T101 and a subsequent rectification tower T102 which are connected in series, wherein a series pipeline is connected with a tower bottom discharge hole of the preorder rectification tower T101 and a tower bottom feed inlet of the subsequent rectification tower T102, and a heating furnace is arranged on the series pipeline in front of the tower bottom feed inlet of the subsequent rectification tower T102; the device is characterized in that 1 or more than 1 side line coupling material flow pipelines which are connected with the preorder rectifying tower T101 and the subsequent rectifying tower T102 are also arranged above the tower bottom discharge hole of the preorder rectifying tower T101 and the tower bottom feed inlet of the subsequent rectifying tower T102; more than 1 complete thermal coupling stripping tower is arranged on one side of the subsequent rectifying tower T102, and more than 1 reflux device is arranged on the other side; the complete thermal coupling stripping tower is provided with 2 pipelines at the top and the bottom respectively to be connected with the subsequent rectifying tower T102, and the middle part is provided with a lateral line product extraction pipeline.
2. The thermally coupled rectification device according to claim 1, characterized in that 1 side-coupled material flow pipeline is arranged between the preceding rectification column T101 and the subsequent rectification column T102;
preferably, the subsequent rectification column T102 is connected to the side-coupled stream line at a position not lower than the middle portion;
preferably, the subsequent rectification column T102 is provided with 1 overhead reflux, 1 or more mid-section reflux;
more preferably, the subsequent rectifying tower T102 is sequentially provided with 1 overhead reflux and 2 middle reflux from top to bottom;
it is also preferred that the overhead reflux stream is withdrawn from 1 to 2 trays below the top of the subsequent rectification column T102 and that the stream is returned to the column at tray 1 of the subsequent rectification column T102.
3. Thermally coupled rectifying device according to claim 1 or 2, characterized in that said subsequent rectifying column T102 may comprise 2 or 3 stripping columns; the top of the stripping tower is connected with the subsequent rectifying tower T102 through two pipelines, and the bottom of the stripping tower is provided with a steam inlet pipeline and a side product output pipeline.
4. The thermally coupled rectification device according to any one of claims 1 to 3 characterized in that the bottom of the subsequent rectification column T102 is further provided with a vapor inlet line;
preferably, the subsequent rectifying tower T102 is provided with a water or non-condensable steam extraction line at the top of the tower;
preferably, the subsequent rectifying tower T102 is provided with a side product output pipeline at the 1 st to 2 nd tower plates.
5. A rectification process based on the thermally coupled rectification device of any one of claims 1 to 4, comprising the following specific process flows:
(1) separation in a preceding rectification column T101
The material to be separated enters the preorder rectifying tower T101 after being heated, light fraction is obtained from the top of the preorder rectifying tower T101, a side-draw material flow of the preorder rectifying tower T101 directly enters the subsequent rectifying tower T102 through a side-coupled material flow pipeline without being heated, and a bottom material of the preorder rectifying tower T101 flows through the series pipeline and is heated by the heating furnace and then enters the subsequent rectifying tower T102;
(2) superheated steam enters the bottom of the subsequent rectifying tower T102 and the bottom of the stripping tower through the steam inlet pipeline respectively to provide heat for the vaporization of a stream in the tower;
(3) separation in the subsequent rectification column T102
Heating the bottom material flow of the preorder rectifying tower T101, then carrying out steam stripping on the bottom material flow in the subsequent rectifying tower T102, taking unvaporized liquid phase as heavy fraction to be extracted from the bottom of the T102, enabling a gas phase material flow to ascend from a lower tower plate, continuously carrying out gas-liquid exchange with the liquid phase below an upper tower plate, recovering the heat in the tower through middle-section reflux and tower top reflux, simultaneously enabling part of the gas phase material flow to enter the complete thermal coupling stripping tower and the stripping tower for steam stripping, and finally respectively obtaining different side line products from the position close to the top of the subsequent rectifying tower, the middle part of the complete thermal coupling stripping tower and the bottom of the stripping; and water or non-condensable vapor is produced at the top of the subsequent rectifying tower.
6. Rectification process according to claim 5, characterized in that the preceding rectification column T101 and the subsequent rectification column T102 are atmospheric or vacuum columns;
preferably, the theoretical plate number of the preorder rectifying tower T101 is more than or equal to 5; more preferably, the number of theoretical plates of the preceding rectifying column T101 is 5-10.
Preferably, the theoretical plate number of the subsequent rectifying tower T102 is not less than 15, and more preferably, when 4 side products and 1 tower bottom heavy fraction are obtained simultaneously, the theoretical plate number of the subsequent rectifying tower T102 is 24-28;
also preferably, the number of theoretical plates of the fully thermally coupled stripping column or stripper column is 4 to 6.
7. The rectification process according to claim 5, wherein the heating furnace outlet temperature is no greater than 390 ℃.
8. The rectification process according to claim 5, wherein the flow rate of the coupled gas phase stream between the subsequent rectification column T102 and the fully thermally coupled stripping column is less than or equal to 1100kg/h, more preferably 900 to 1100kg/h, and the flow rate of the coupled liquid phase stream is about 24100 to 2450 kg/h.
9. The rectification process according to claim 5, wherein the top reflux flow rate of the subsequent rectification column T102 is 30000-45000 kg/h, the first mid-section reflux flow rate is 10000-20000 kg/h, and the second mid-section reflux flow rate is 20000-30000 kg/h from top to bottom.
10. Use of the rectification process as claimed in any one of claims 5 to 9 in atmospheric and vacuum distillation of crude oil, cutting of secondary processed oils;
specifically, the cutting of the secondary processed oil product comprises the cutting of a catalytic cracking product into gasoline and diesel oil, and the cutting of the oil product subjected to the hydrotreatment into the gasoline, the diesel oil and various grades of hydrogenated base oil.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911104596.9A CN112791435A (en) | 2019-11-13 | 2019-11-13 | Thermal coupling rectification device and thermal coupling rectification process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911104596.9A CN112791435A (en) | 2019-11-13 | 2019-11-13 | Thermal coupling rectification device and thermal coupling rectification process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN112791435A true CN112791435A (en) | 2021-05-14 |
Family
ID=75803134
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911104596.9A Pending CN112791435A (en) | 2019-11-13 | 2019-11-13 | Thermal coupling rectification device and thermal coupling rectification process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112791435A (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1344780A (en) * | 2000-09-25 | 2002-04-17 | 王仲华 | Normal pressure pregasifying and several section amterial feeding process of crude oil distiller |
| CN101475826A (en) * | 2008-11-21 | 2009-07-08 | 华东理工大学 | Atmospheric vacuum distillation process for light crude oil |
| CN101890249A (en) * | 2010-07-22 | 2010-11-24 | 蓝仁水 | Energy-saving process method for rectifying and separating three fractions |
| CN102641604A (en) * | 2012-04-01 | 2012-08-22 | 中国石油化工股份有限公司 | Multiple-component lateral line thermal coupling rectification method |
| US20150122704A1 (en) * | 2013-11-01 | 2015-05-07 | Council Of Scientific And Industrial Research | Method for increasing gas oil yield and energy efficiency in crude oil distillation |
| CN108467744A (en) * | 2018-03-27 | 2018-08-31 | 天津大学 | A kind of the subtracting five line product method for upgrading of Lube Type decompression partitioned column |
-
2019
- 2019-11-13 CN CN201911104596.9A patent/CN112791435A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1344780A (en) * | 2000-09-25 | 2002-04-17 | 王仲华 | Normal pressure pregasifying and several section amterial feeding process of crude oil distiller |
| CN101475826A (en) * | 2008-11-21 | 2009-07-08 | 华东理工大学 | Atmospheric vacuum distillation process for light crude oil |
| CN101890249A (en) * | 2010-07-22 | 2010-11-24 | 蓝仁水 | Energy-saving process method for rectifying and separating three fractions |
| CN102641604A (en) * | 2012-04-01 | 2012-08-22 | 中国石油化工股份有限公司 | Multiple-component lateral line thermal coupling rectification method |
| US20150122704A1 (en) * | 2013-11-01 | 2015-05-07 | Council Of Scientific And Industrial Research | Method for increasing gas oil yield and energy efficiency in crude oil distillation |
| CN108467744A (en) * | 2018-03-27 | 2018-08-31 | 天津大学 | A kind of the subtracting five line product method for upgrading of Lube Type decompression partitioned column |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108101748B (en) | Four-tower three-effect methanol rectification energy-saving process method and device | |
| JPS5824301A (en) | Distillation method | |
| CN102234541A (en) | Energy-saving pyrolysis gasoline full-cut hydrogenation method and device | |
| CN102234540B (en) | Hydrogenation method and apparatus for center fractions of pyrolysis gasoline | |
| CN100348286C (en) | Double tower gas fractionator and fractional method | |
| CN207047164U (en) | A kind of following light component piece-rate systems of reformed oil C5 | |
| CN109646980B (en) | Fusel-free oil dividing wall tower coupled methanol multi-effect rectification energy-saving device and method | |
| CN109762590B (en) | Fractionation system and fractionation method | |
| CN103611328A (en) | Process for extracting naphthalene by continuously rectifying heavy benzol | |
| CN201686667U (en) | Cracking gasoline full-fraction hydrogenation device | |
| CN114989856A (en) | Method and device for separating aromatic hydrocarbon or sulfur-containing compound from gasoline fraction | |
| CN102641604B (en) | A kind of process of multicomponent side line thermal coupling rectification | |
| CN112791435A (en) | Thermal coupling rectification device and thermal coupling rectification process | |
| CN103896702B (en) | Light hydrocarbon separation method and system from middle precut of fraction | |
| CN201686666U (en) | Middle-fraction hydrogenation device of cracked gasoline | |
| CN103664453A (en) | Light hydrocarbon separation method for applying pasteur rectification to deethanization-ethylene fractionation | |
| CN106582053B (en) | The process and device of the tower methanol distillation column by-product ethyl alcohol of partition | |
| CN1030070A (en) | Single tower debenzolizing process and novel debenzolizing tower | |
| CN105646147B (en) | A kind of Methanol Recovery method | |
| CN1304343C (en) | Method and device for separating 1,2,3-trimethylbenzene | |
| CN1061080C (en) | Crude oil atmospheric vacuum rectifying process with extractive distillation zone | |
| Cui et al. | Intensifying petroleum fractionators through internal partial condensation in place of pump-around | |
| CN111939584A (en) | Process and system for evaporating crude benzene in benzene hydrogenation reaction system | |
| CN105087065A (en) | Pyrolysis gasoline central fraction hydrogenation device and method thereof | |
| CN106318435A (en) | Normal pressure distillation method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |