CN111560273B - Chilling tower for separating Fischer-Tropsch synthesis products and process system thereof - Google Patents
Chilling tower for separating Fischer-Tropsch synthesis products and process system thereof Download PDFInfo
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- CN111560273B CN111560273B CN202010166488.0A CN202010166488A CN111560273B CN 111560273 B CN111560273 B CN 111560273B CN 202010166488 A CN202010166488 A CN 202010166488A CN 111560273 B CN111560273 B CN 111560273B
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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Abstract
The invention relates to a chilling tower for separating Fischer-Tropsch synthesis products and a process system thereof, which comprise a chilling tower body, a main feeding system, an auxiliary feeding system, a heat exchange element, a spraying washing system and a tower tray system, wherein the upper part in the chilling tower body is a gas phase area, the lower part in the chilling tower body is a liquid phase area, the main feeding system is arranged in the gas phase area, the spraying washing system and the tower tray system are sequentially arranged above the main feeding system, and the auxiliary feeding system and the heat exchange element are arranged in the liquid phase area. Compared with the prior art, the gas-phase product of the Fischer-Tropsch synthesis reactor is washed, cooled and distilled for many times in the chilling tower, so that the light oil and the heavy oil are effectively separated from the Fischer-Tropsch synthesis, and the chilling tower has the characteristics of reasonable design structure and layout, high product separation efficiency, high operation flexibility, simple process system, small system resistance, high heat energy recovery efficiency and the like, and is more suitable for the operation of a large Fischer-Tropsch synthesis process system.
Description
Technical Field
The invention belongs to the field of chemical equipment devices, and particularly relates to a chilling tower for separating Fischer-Tropsch synthesis products and a process system thereof.
Background
The Fischer-Tropsch synthesis reaction is a typical catalytic exothermic reaction, one of the catalysts which are commonly used at present is an iron-based catalyst, the other catalyst is a cobalt-based catalyst, the two catalysts are in the form of fine solid particles, and the particle size is 0-250 mu m. The chilling tower is one of important equipment of a Fischer-Tropsch synthesis system, and is mainly used for separating heavy oil and light oil in Fischer-Tropsch synthesis gas phase products and recovering heat energy carried in the Fischer-Tropsch synthesis gas phase products.
The gas phase product of Fischer-Tropsch synthesis has high temperature and carries some fine solid catalyst particles, so that the gas phase product is easy to deposit and block in the separating system to affect the separating effect. The conventional chilling tower structure has unreasonable internal components, uneven fluid distribution, poor separation effect and easy blockage of solids. In the conventional separation process, a waste heat boiler is generally arranged in front of a chilling tower to pre-cool a gas-phase product, a heat exchanger is arranged outside the chilling tower to cool a circulating liquid or extracted heavy oil, and the like, so that the problems that monomer heat exchange equipment is large in size, low in heat energy utilization efficiency, the waste heat boiler and a heat exchanger are easy to block and the like exist, especially for large and high-temperature Fischer-Tropsch synthesis devices, the problems are more prominent, and the large-scale operation of the Fischer-Tropsch synthesis process technology is severely limited.
The system for solving the problems is very important for realizing continuous and stable operation and scale-up of the Fischer-Tropsch synthesis device.
Disclosure of Invention
The invention aims to solve the problems, provides a chilling tower for separating Fischer-Tropsch synthesis products and a process system thereof, aims to solve the problems of uneven fluid distribution in the chilling tower, incomplete product separation, easy deposition and blockage of solids, low heat energy recovery utilization rate of the system, unstable operation and the like, and is particularly suitable for the design and operation of large-scale Fischer-Tropsch synthesis product separation equipment and process.
The purpose of the invention is realized by the following technical scheme:
the utility model provides a quench tower for separation of ft synthesis result, includes quench tower body, main charge-in system, supplementary charge-in system, heat exchange element, sprays washing system and tray system, this internal upper portion of quench tower is the gaseous phase region, and the lower part is the liquid phase region, main charge-in system sets up in the gaseous phase region, it sets gradually with the tray system to spray washing system the top of main charge-in system, supplementary charge-in system and heat exchange element set up in the liquid phase region.
Gas-phase products of the Fischer-Tropsch synthesis reaction enter a chilling tower body from a main feeding system and an auxiliary feeding system, the spraying and washing system is used for washing and cooling gas rising in the tower in a gas-phase area of the chilling tower body, part of heavy oil in the gas-phase products is condensed into liquid which enters washing liquid and falls into liquid-phase products at the bottom of the tower, and meanwhile solid catalyst particles carried in the gas-phase products also enter the liquid phase; the tray system above the spraying and washing system further washes, cools and separates the ascending gas, wherein each tray in the tray system carries out mass transfer of gas-liquid two phases, the light component is continuously evaporated to enter a gas phase, and the heavy component is continuously condensed to enter a liquid phase, so that the effective separation of the light oil and the heavy oil is realized; in the liquid phase region of the chilling tower body, the heat exchange element recycles heat energy, and a gas-phase product of the auxiliary feeding system bubbles the upper part of the liquid phase region, so that the heat transfer of the heat exchange element is enhanced, and the heat exchange efficiency is improved.
The invention realizes that the gas-phase product of the Fischer-Tropsch synthesis reaction is washed, cooled and distilled for many times in the chilling tower body, realizes the effective separation of Fischer-Tropsch synthesis light oil and heavy oil, and effectively recycles the heat energy carried in the gas-phase product of the Fischer-Tropsch synthesis reaction.
As a preferable technical scheme, the chilling tower body is a cylindrical barrel. The chilling tower body of the invention is a cylindrical barrel with the size determined according to the designed production scale and the technological operation conditions, and the diameter of the barrel of the chilling tower can be consistent up and down or different in diameter up and down according to the requirements of fluid load and fluid distribution in different areas. As an optimized design of the invention, the chilling tower with the diameter of the lower part enlarged is more suitable for a product separation system of a high-temperature and large-scale Fischer-Tropsch synthesis device.
The main feeding system comprises a pipeline outside the chilling tower and a pipeline extending into the chilling tower, wherein the pipeline inside the chilling tower extends from one end to the other end along the radial center line of the tower, one or more notches are formed in the inner pipe section downwards, the one or more notches are symmetrically arranged relative to the center of the tower section and are uniformly distributed, and gas flows out downwards in the pipeline and uniformly fills the tower section, and then turns to flow upwards in a baffling mode.
As a preferable technical scheme, the auxiliary feeding system comprises an auxiliary feeding pipeline, a gas distributor and a support piece thereof, wherein the gas distributor adopts a tubular distribution structure and comprises a gas inlet main pipe, a gas distribution branch pipe of a fishbone structure and a gas nozzle welded on the branch pipe.
As a preferable technical scheme, the direction of the gas nozzle is designed to be vertical downward, the size of the inner diameter of the nozzle ensures that the pressure drop generated by the gas passing through each nozzle of the distribution pipe is between 0.005 and 0.05MPa, and the aperture of the gas nozzle is between 5 and 25 mm. And the gas flows out of the nozzle at the speed of 2-10 m/s and then flows upwards in a baffled manner, and flows upwards in a uniform and fine bubble manner in a liquid phase region at the lower part of the chilling tower, so that good disturbance is formed on the liquid phase region, and the mass transfer and heat transfer of the liquid are enhanced.
As an optimal technical scheme, the air input of the auxiliary feeding system is 5-50%, preferably 10-30% of the total gas amount of the gas-phase product of the Fischer-Tropsch synthesis, and the rising speed of the gas in the liquid phase at the lower part of the tower is controlled to be 0.1-0.6 m/s.
As a preferable technical scheme, the heat exchange element is a heat exchange tube, one or more layers of heat exchange tubes are arranged, the number of the heat exchange tubes is gradually reduced from top to bottom so as to adapt to heat transfer loads in different areas.
The heat exchange tube comprises one or more of a spiral coil heat exchange tube, a circuitous multi-pass heat exchange tube or a tube array heat exchange tube.
The heat exchange elements are all arranged in the liquid phase area of the chilling tower body, and the heavy oil at the lower part of the chilling tower is cooled by adopting a cooling medium in the heat exchange tubes. The heat exchange tube can be in the following three types: one is a spiral coil type heat exchange tube, which is a coil concentric with a chilling tower for a plurality of circles or a plurality of coils with axes parallel to the central axis of the tower, wherein a heat exchange medium spirally flows from bottom to top in the coil; one is a circuitous multi-pass heat exchange tube, a plurality of vertical or horizontal heat exchange tubes are combined together through connecting elbows, liquid in each group of heat exchange tubes flows in a circuitous way up and down or left and right, and a plurality of groups of heat exchange tubes can be arranged; the other type is a tube array type heat exchange tube, a plurality of heat exchange tubes are connected to a water distribution pipeline, the heat exchange tubes are converged to a header pipe after heat exchange, and a heat exchange medium flows in the tubes in a single way from bottom to top. The circuitous multi-pass and tube array heat exchange tubes can adopt the forms of spiral flat tubes, corrugated tubes, pin fin tubes or finned tubes and the like to carry out enhanced heat exchange. The multilayer heat exchange tube in the invention can be any combination of the above types.
The cooling medium and the cooling mode of the heat exchange tube can be but not limited to heating boiler cooling water, and the steam drum byproduct steam is arranged, the feed gas is subjected to heating pretreatment and cooling by adopting circulating cooling water, wherein the heavy oil is cooled and cooled preferentially by adopting a mode capable of recovering heat energy.
As a preferred technical scheme, the spraying and washing system is arranged into one or more layers and comprises a liquid distribution pipe, and a plurality of liquid injection holes are formed in the middle lower part of the liquid distribution pipe. In order to ensure the effectiveness of product separation, liquid with a component similar to that of heavy oil is preferably used as a washing liquid, such as heavy oil at the bottom of a chilling tower, clean heavy oil and clean light oil, but not limited to the above liquids;
as a preferred technical scheme, the liquid distribution pipes are in a shark fin structure, the distribution pipes of two adjacent layers are staggered, the liquid jet holes are uniformly distributed on two sides of the central line of the distribution pipes, and the included angle of the liquid distribution pipes of the two adjacent layers is 90 degrees, so that gas channeling can be effectively prevented, and gas-liquid contact is strengthened;
the included angle of the central lines of the spraying holes distributed on the two sides of the central line of the liquid distribution pipe is 20-140 degrees, the preferred design included angle is 30-90 degrees, the liquid spraying holes have the functions of atomization and uniform distribution on the washing liquid, the washing liquid is atomized by the spraying holes and is sprayed obliquely downwards at high speed to be in full contact with gas phase materials rising in the tower, solid particles carried in the gas phase materials are washed, the gas phase materials are cooled, and meanwhile heavy oil in the gas phase products is cooled to become liquid and flows downwards along with the washing liquid.
As a preferred technical scheme, the tray system comprises one or more layers of trays, the tray form can be but is not limited to a valve tray, a valve tray or a sieve tray, a liquid feeding pipeline is arranged above the trays, and the feeding liquid can be but is not limited to heavy oil, liquid light oil and clean heavy oil liquid phase material after filtration treatment at the bottom of a chilling tower. On each tray, liquid and gas are in full contact to perform good mass transfer and heat transfer, light components are continuously evaporated to enter a gas phase, heavy components are continuously condensed to enter a liquid phase, and effective separation of light oil and heavy oil is realized. Furthermore, the preferable number of the tower trays of the tower tray system for washing and separating is 3-9 blocks.
As a preferable technical scheme, a liquid-solid separation tank is further arranged at the lower part of the liquid phase region of the chilling tower, the liquid-solid separation tank comprises a bottom plate, a top plate, an outer partition plate and an inner partition plate, the bottom plate, the outer partition plate and a barrel of the chilling tower form a liquid accumulation chamber with an opening at the upper part, and the lower part of the liquid accumulation chamber is connected with a liquid discharge port;
the top plate, the inner partition plate and the barrel of the chilling tower form a cover body with an opening at the lower part, the cover body is arranged at the upper part of the liquid accumulation chamber, and a liquid flow passage with an inlet positioned at the bottom of the liquid accumulation chamber is formed between the inner partition plate and the outer partition plate.
In a liquid phase area at the lower part of the chilling tower, liquid carries solid to flow from top to bottom, liquid turns to flow upwards to enter a liquid accumulating chamber in a liquid flow passage formed between an inner partition plate and an outer partition plate, and the carried solid particles continue to flow downwards under the action of gravity, so that liquid-solid separation is effectively realized. The liquid without solid in the liquid accumulation chamber can flow out from the liquid discharge hole and enter the liquid circulation system.
As a preferred technical scheme, the inner partition plate and the outer partition plate are both vertically arranged and have a distance therebetween, the upper part of the outer partition plate and the top plate have a distance therebetween, the top plate and the bottom plate are welded on the tower wall by adopting steel plates, the inner partition plate is welded on the top plate, the outer partition plate is welded on the bottom plate, the projection of the top plate is larger than that of the bottom plate, the top plate is horizontally or obliquely arranged, and for solid-containing liquid, the downward-inclined top plate is preferentially adopted, so that the flow of the solid-containing liquid is facilitated, and the solid deposition is prevented; the vertical partition plate can be in the form of a circular arc partition plate or a square partition plate, and preferably a circular partition plate.
As a preferable technical scheme, a pressure balance pipe is arranged between the top of the liquid-solid separation tank and a gas phase area of the chilling tower. The pressure balance pipe can be arranged inside the tower or outside the tower, and the pipe orifice of the pressure balance pipe in the gas phase area of the chilling tower can be designed to be horizontal, inclined downwards or vertically upwards. When a vertically upward pipe orifice is adopted, a top cap is arranged above the pipe orifice to prevent gas backflow or liquid backflow.
As a preferable technical scheme, the chilling tower is also provided with one or more groups of liquid circulating systems, each liquid circulating system comprises a circulating pipeline and a pressure raising pump, the inlet of each circulating pipeline is connected with the liquid phase area at the bottom of the chilling tower or the liquid discharge port of the liquid-solid separation tank, and the outlet of each circulating pipeline is connected with the spray washing system and/or the tray system.
The liquid circulating system conveys the heavy oil at the bottom of the chilling tower to the middle part and the upper part of the chilling tower again to be used as a washing liquid of a spraying washing system and a tower tray system, and gas-phase materials are washed and cooled; the liquid discharge port is arranged in a liquid phase area at the lower part of the chilling tower and can be arranged above, in the middle or below the heat exchange element according to different temperatures of the circulating liquid; the liquid feeding port is arranged in a gas phase area at the middle upper part of the chilling tower and is connected with a liquid spraying device or a liquid feeding pipeline above the tower tray, and the heavy oil at the tower bottom is used for supplying liquid for the washing spraying device and/or the separation tower tray.
As a preferable technical scheme, the top of the chilling tower is provided with a light oil discharging system which comprises a demister and a discharging pipeline, and the demister is arranged on the inner side of the top of the chilling tower. The demister can be of a type including, but not limited to, wire mesh type, vane type, plate type (baffle, plate, etc.), tube bundle type, etc., and the wire mesh type is preferably used in the present invention. And (4) removing entrained liquid from the light oil and the tail gas at the top of the chilling tower through a demister, and conveying the light oil and the tail gas to a subsequent procedure for continuous processing.
As a preferable technical scheme, a heavy oil discharging system is arranged at the bottom of the chilling tower and comprises a heavy oil discharging port, a pipeline, a flash tank, a filter, a storage tank and a pressure raising pump.
A process system for Fischer-Tropsch synthesis product separation comprises the chilling tower, a flash evaporator, a filter, a heavy oil storage tank and a pressure raising pump, and the specific process comprises the following steps:
gas-phase products from the top of the Fischer-Tropsch synthesis reactor enter a chilling tower through a main feeding system and an auxiliary feeding system, and light oil and reacted tail gas are sent to a post-process treatment through a tower top discharging system of the chilling tower in the form of gas-phase products;
and a part of the liquid phase heavy oil at the bottom of the chilling tower is sent to a liquid circulating system to be used as a washing liquid of a chilling tower spray washing system and/or a tray system, a part of the liquid phase heavy oil is extracted from the bottom of the tower to enter a tower bottom discharging system, light components are removed through a flash evaporator, solid particles are removed through a filter, the liquid phase heavy oil enters a heavy oil storage tank, the heavy oil is pressurized through a pressure raising pump and then is sent to a refining process, and/or a part of clean heavy oil is sent to the upper part of the chilling tower to be used as a washing liquid of the chilling.
As a preferable technical scheme, raw material gas of Fischer-Tropsch synthesis reaction is used as a heat exchange medium to exchange heat with light oil and tail gas in the gas phase at the top of a chilling tower, part of heat energy is recovered, the heat energy is sent to a heat exchanger at the lower part of the chilling tower to recover the heat energy of heavy oil, and the preheated raw material gas is sent to a Fischer-Tropsch synthesis reactor to react.
As an optimized technical scheme, the temperature of gas-phase product feeding of the Fischer-Tropsch synthesis reaction is 210-430 ℃, the operating pressure is 1.5-5.0 MPa, the temperature of the top of a chilling tower is 120-230 ℃, the temperature of cooled heavy oil is 120-200 ℃, and the resistance of the chilling tower is less than 70 KPa.
The chilling tower and the internal components of the invention have reasonable design structure, uniform fluid distribution, good mass transfer and heat transfer effects, high heat recovery rate, simple process flow and stable and reliable operation, systematically solve the problems of huge monomer heat exchanger, low heat efficiency, easy blockage, poor separation effect, unstable operation and the like of the existing product separation system, and are more suitable for large-scale and large-scale design and operation of a Fischer-Tropsch synthesis device.
Drawings
FIG. 1 is a schematic diagram of a Fischer-Tropsch synthesis product separation system process flow;
FIG. 2 is a schematic diagram of a quench tower configuration;
FIG. 3 is a schematic diagram of a quench tower having a reduced diameter and an external balance tube;
FIG. 4 is a top view of a gas distributor of the auxiliary feed system;
FIG. 5 is a top view of a spray washing system with two adjacent layers;
FIG. 6 is a schematic view of the structure of the liquid-solid separation apparatus;
FIG. 7 is a schematic diagram of a Fischer-Tropsch synthesis product separation system without a heat exchanger outside a quench tower;
FIG. 8 is a schematic view of a Fischer-Tropsch synthesis product separation system with a heat exchanger disposed outside the quench tower.
Detailed Description
The following embodiment is a Fischer-Tropsch product separation system for producing liquid fuel from syngas, and will now be described by way of example with reference to the accompanying drawings. The following embodiments and drawings are only for the understanding of the present invention and do not limit the present invention in any way.
FIG. 1 is a quench tower system and process flow for Fischer-Tropsch synthesis product separation, the system comprising: the gas phase product from the top of the Fischer-Tropsch synthesis reactor enters the chilling tower through the main and auxiliary feeding systems 2 and 3, the heavy oil is condensed and separated from the gas phase product and then enters the tower bottom, and solid particles carried in the gas phase product are washed by the spraying washing liquid and then enter the liquid phase product at the tower bottom. The light oil and the tail gas after reaction are sent to a post-process treatment through a tower top discharging system in the form of gas-phase products. The liquid phase heavy oil at the bottom of the tower is cooled by the heat exchange elements 5 and 6, then the part of the liquid phase heavy oil is sent to a liquid circulation system to be used as a spray washing liquid and a tower tray washing liquid of the chilling tower, the part of the liquid phase heavy oil is extracted at the bottom of the tower to enter a tower bottom discharging system, light components are removed by a flash evaporator, solid particles are removed by a filter, then the liquid phase heavy oil enters a heavy oil storage tank, the heavy oil is pressurized by a pressure raising pump and then sent to a refining procedure, and the part of.
Fig. 2 and 3 are schematic diagrams of design structures of a quench tower, two layers of heat exchange elements 5 and 6 are arranged in a liquid phase region at the lower part of the quench tower shown in fig. 2, wherein the heat exchange element at one layer adopts a form of boiler water evaporation byproduct steam for heat exchange, the heat exchange element at the second layer adopts a mode of preheating feed gas for heat exchange, and the heat exchange elements at the two layers both recycle heat energy. The main feeding system 2 of the feeding system is arranged above a liquid phase region of the chilling tower, the auxiliary feeding system 3 is arranged between a first layer and a second layer of heat exchange elements of the liquid phase region, and a gas phase product of the auxiliary feeding system bubbles the upper part of the liquid phase region, so that the heat transfer of the first layer of heat exchange elements can be enhanced, and the heat exchange efficiency is improved. Two groups of spraying and washing systems 7, 8, 9 and 10 are arranged above the main feeding system, gas rising in the tower is washed and cooled, and part of heavy oil in the gas-phase product is condensed into liquid, enters the washing liquid and falls into the liquid-phase product at the bottom of the tower. Simultaneously, the solid catalyst particles carried in the gas phase product also enter the liquid phase. In fig. 2, the quench tower is provided with 6 trays 13 above the spray scrubbing system for further scrubbing, temperature reduction and separation of the rising gas. Two inlets 11, 12 for scrubbing liquid are provided in the upper part of the tray to supply scrubbing liquid to the tray. Meanwhile, gas-liquid two-phase mass transfer is carried out on each tray, light components are continuously evaporated to enter a gas phase, heavy components are continuously condensed to enter a liquid phase, and effective separation of light oil and heavy oil is realized. The top of the column is provided with a light oil and off-gas outlet 15 and the bottom of the column is provided with a heavy oil outlet 20. A demister 14 is provided in front of the top outlet of the column for gas-liquid separation to prevent the liquid from being entrained in the top gas phase. In fig. 2, two groups of liquid circulation systems of the quench tower are arranged, the liquid phase region of the quench tower barrel 1 is provided with two circulation liquid outlets, one is a circulation liquid outlet 17 in the tower, and the other is a circulation liquid outlet 19 at the bottom of the tower, wherein a liquid-solid separation tank 16 is arranged in front of the circulation liquid outlet 17 in the tower, and the specific structure is shown in fig. 6.
In the design of the invention, the diameter of the part of the chilling tower can be enlarged or reduced according to the gas phase load of different areas of the chilling tower and the arrangement requirement of the components in the tower. FIG. 3 shows a schematic diagram of a quench tower having a large lower diameter and a small upper diameter.
Fig. 4 is a top view of the distribution pipe of the auxiliary feeding system, and the gas distribution pipe is designed to prevent the gas from generating rotational flow, channeling or short flow in the liquid phase by considering the uniformity of gas distribution. Depending on the size of the quench tower diameter, the gas distribution plate 4 may be arranged in one or more groups, shown in FIG. 4 as group 1. The gas distribution plate 4 includes a main inlet pipe 21, a shark fin-shaped distribution pipe 22, gas nozzles 23, and a support 24. The main air inlet pipe 21 and the shark fin-shaped distribution pipes 22 are horizontally arranged, the shark fin distribution pipes 22 are a plurality of groups of branch pipes symmetrically arranged on the left and right of the main air inlet pipe, and the central lines of the shark fin distribution pipes 22 and the main air inlet pipe 2 are on the same horizontal plane. The gas nozzles 23 are a plurality of vertical downward short pipes welded on the shark fin distribution pipeline 22, the central line of the vertical downward nozzle is vertically intersected with the central line of the shark fin distribution pipeline 22, the gas nozzles are uniformly distributed on the cross section of the tower, and the size and the number of the pore diameters of the gas nozzles are ensured to ensure that the pressure drop generated by the gas passing through each nozzle of the distribution pipeline is between 0.005 and 0.05 MPa. The gas vertically and downwards enters the chilling tower through the nozzle, is uniformly distributed in a liquid phase in a fine bubble form, flows upwards in a baffling mode, effectively disturbs the liquid phase in a heat exchange area, and improves the heat exchange efficiency. The support member 24 is welded and fixed on the shell of the chilling tower, and mainly plays a role in supporting and fixing the main air inlet pipe 21 and the shark fin-shaped distribution pipe 22. In the present invention, alternative materials for the support 24 include, but are not limited to, i-section steel, channel steel, or other section steel.
FIG. 5 is a top view of a liquid spray washer with two adjacent layers, with spray feed lines and manifolds intersecting at 90.
Fig. 6 shows a schematic of the structure of the liquid-solid separation device 16, and the liquid-solid separation device 16 includes a top plate 25, a bottom plate 26, an inner partition 27, an outer partition 28, a liquid accumulation chamber 29, and an equilibrium line 18. A top plate 25 and a bottom plate 26 are welded to the quench drum 1, an inner partition plate 27 is welded to the top plate 25, and an outer partition plate 28 is welded to the bottom plate 26.
In the present invention, the outer baffle 28, the floor 26 and the quench drum 1 of the liquid-solid separation device 16 form an open-topped vessel, namely, a liquid accumulation chamber 29. The inner partition 27, the top plate 25 and the quench drum 1 form an open-bottomed vessel which is surmounted by a liquid accumulation chamber 29 from above. A gap is reserved between the upper part of the liquid accumulating chamber 29 and the top plate 25, and a gap is reserved between the inner partition plate 27 and the outer partition plate 28, wherein the size of the gap is required to meet the requirement of flowing of the circulating liquid in the liquid accumulating chamber 29. The lower part or the bottom of the liquid accumulation chamber 29 is connected with a liquid outlet of the liquid circulation system. Fig. 6 also shows the flow pattern of the liquid-solid separation tank 16, in the liquid phase region in the quench tower, the liquid flows from top to bottom, at the liquid-solid separation device 16, the solid-containing liquid flows downwards along the top plate 25 and the inner partition plate 27, the liquid turns to flow upwards through the gap between the inner partition plate 27 and the outer partition plate 28, the contained solid continues to flow downwards under the action of gravity, the liquid is separated from the solid, the liquid flows into the liquid accumulation chamber along the gap between the inner partition plate and the outer partition plate and the gap between the liquid accumulation chamber and the top plate, and the solid is deposited at the bottom of the tower.
In the invention, a pressure balance pipeline 18 is also arranged between the top of the liquid-solid separation device 16 and a gas phase area of the chilling tower, the balance pipeline 18 is arranged inside the chilling tower in the figures 1 and 6, an outlet of the gas phase area is vertically upward, a top cap 30 is arranged above the outlet, the projection of the top cap 30 is designed to be larger than that of the balance pipeline so as to prevent gas or liquid from flowing backwards, and the form of the top cap is not limited. The equalization line 18 shown in FIG. 2 is disposed outside of the quench tower, with the exit of the equalization line in the gas phase region being vertically downward.
Example 1
A process system for separating Fischer-Tropsch synthesis products is disclosed, the process flow is shown in figure 7, gas phase products with the temperature of about 320 ℃ from the top of a Fischer-Tropsch synthesis reactor enter a chilling tower through a main feeding system and an auxiliary feeding system, heavy oil is condensed and separated from the gas phase products and then enters the tower bottom after being sprayed, washed and cooled, and the solid particles carried in the gas phase products are also washed and then enter the liquid phase products at the tower bottom after being sprayed, washed and separated. The light oil and the tail gas after reaction are sent to a post-process treatment through a tower top discharging system in the form of gas-phase products. After being cooled by a heat exchange element, part of liquid-phase heavy oil at the bottom of the tower is sent to a liquid circulation system to be used as a spray washing liquid and a tower tray washing liquid of the chilling tower, and part of the liquid-phase heavy oil is extracted at the bottom of the tower to enter a tower bottom discharging system, light components are removed through a flash evaporator, solid particles are removed through a filter, the liquid-phase heavy oil enters a heavy oil storage tank, the heavy oil is pressurized through a pressure raising pump and then sent to a refining process, and part of clean heavy oil is.
In the process, raw gas and drum make-up water are adopted to recover heat, and the temperature of heavy oil is reduced. The raw material gas exchanges heat with the light oil and the tail gas in the gas phase at the top of the tower, then exchanges heat with a first-stage heat exchanger arranged in a chilling tower, reduces the temperature of heavy oil at the bottom of the tower, and the gas after heat exchange enters a Fischer-Tropsch synthesis reactor and passes through a steam drum to produce a byproduct of 4.4MPa steam together with reaction heat. And the steam drum supplementing water is adopted in a secondary heat exchanger inside the chilling tower to continuously cool the heavy oil, and the steam drum supplementing water at the temperature of 104 ℃ is sent to the steam drum after heat exchange and temperature rise so as to improve the steam generation rate of the steam drum. The steam pocket supplementary water is provided with a secondary line, and the temperature of the heavy oil at the bottom of the tower is adjusted by adjusting the flow of the steam pocket supplementary water. The process recovers heat through graded heat exchange, the temperature of feed gas at the inlet of the reactor is raised, and the recovered heat is converted into high-quality steam in the reactor.
Example 2
A process system for separating Fischer-Tropsch synthesis products is disclosed, the flow is as shown in figure 8, gas phase products with the temperature of about 345 ℃ from the top of a Fischer-Tropsch synthesis reactor enter a chilling tower through a main feeding system and an auxiliary feeding system, heavy oil is condensed and separated from the gas phase products and then enters the tower bottom after being sprayed, washed and cooled, tray washing and cooling, and solid particles carried in the gas phase products are also washed and then enter liquid phase products at the tower bottom after being sprayed, washed and separated. The light oil and the tail gas after reaction are sent to a post-process treatment through a tower top discharging system in the form of gas-phase products. After being cooled by a heat exchange element, part of liquid-phase heavy oil at the bottom of the tower is sent to a liquid circulation system to be used as a spray washing liquid and a tray washing liquid of the chilling tower, and part of the liquid-phase heavy oil is extracted at the bottom of the tower to enter a tower bottom discharging system, light components are removed through a flash evaporator, solid particles are removed through a filter, then the liquid-phase heavy oil enters a heavy oil storage tank, the heavy oil is pressurized through a pressure raising pump and then sent to a refining process, and part of clean heavy oil can also be.
In the process, raw gas and drum make-up water are adopted to recover heat, and the temperature of heavy oil is reduced. The raw material gas is divided into two paths, one path of raw material gas firstly exchanges heat with light oil and tail gas in the gas phase at the top of the tower, then exchanges heat with a heat exchanger arranged in a chilling tower to reduce the temperature of heavy oil at the bottom of the tower, the other path of raw material gas enters a circulating cooler outside the tower, two paths of raw material gas are combined to enter a Fischer-Tropsch synthesis reactor after exchanging heat, and the two paths of raw material gas pass through a steam drum together with reaction heat to produce 4.4MPa steam as a. And a cooler is connected in series behind the circulating cooler outside the tower, and steam drum supplementary water or circulating hot water is adopted for cooling so as to regulate and control the temperature of the heavy oil. And a cooler is arranged on the heavy oil discharged material at the bottom of the chilling tower to control the temperature, and hot water is adopted for circulating cooling. The steam drum supplementing water at 104 ℃ is sent to the steam drum after heat exchange and temperature rise, and is used for improving the steam production rate of the steam drum. The steam pocket supplementary water is provided with a secondary line, and the temperature of the heavy oil at the bottom of the tower is adjusted by adjusting the flow of the steam pocket supplementary water. The process recovers heat through graded heat exchange, the temperature of feed gas at the inlet of the reactor is raised, and the recovered heat is converted into high-quality steam in the reactor.
Claims (18)
1. A chilling tower for separating Fischer-Tropsch synthesis products is characterized by comprising a chilling tower body, a main feeding system, an auxiliary feeding system, a heat exchange element, a spraying and washing system and a tray system,
the upper part in the chilling tower body is a gas phase area, the lower part in the chilling tower body is a liquid phase area, the main feeding system is arranged in the gas phase area, the spraying washing system and the tower tray system are sequentially arranged above the main feeding system, and the auxiliary feeding system and the heat exchange element are arranged in the liquid phase area;
the heat exchange elements are heat exchange tubes and are arranged in two layers, and the auxiliary feeding system is arranged between the two layers of heat exchange elements;
the air input of the auxiliary feeding system is 5-50% of the total gas amount of the gas-phase product of the Fischer-Tropsch synthesis, and the rising speed of the gas in the liquid phase at the lower part of the tower is controlled to be 0.1-0.6 m/s.
2. A quench tower for use in Fischer-Tropsch synthesis product separation according to claim 1, wherein the quench tower body is a cylindrical drum.
3. A quench tower for Fischer-Tropsch synthesis product separation according to claim 1, wherein the main feed system comprises a line external to the quench tower and a line extending into the quench tower, the line extending from one end to the other along the radial centerline of the tower, and the internal pipe section is notched downwardly, the one or more notches being symmetrically located with respect to the center of the tower cross-section and being evenly distributed so that gas flows down the line and evenly fills the tower cross-section, and is deflected upwardly.
4. A quench tower for Fischer-Tropsch synthesis product separation according to claim 1, wherein the auxiliary feed system comprises an auxiliary feed line, a gas distributor and its support members, the gas distributor is of a tubular distribution structure and comprises a gas inlet header, gas distribution branches of a fishbone structure and gas nozzles welded to the branches.
5. A quench tower for Fischer-Tropsch synthesis product separation according to claim 4, wherein the gas nozzles are oriented vertically downward, the inner diameter of the nozzles is sized to provide a pressure drop of between 0.005 and 0.05MPa for the gas passing through each nozzle of the distributor tube, and the diameter of the gas nozzles is between 5 and 25 mm.
6. A quench tower for Fischer-Tropsch synthesis product separation according to claim 1, wherein the heat exchange tubes comprise one or more combinations of spiral coil heat exchange tubes, circuitous multi-pass heat exchange tubes, or shell and tube heat exchange tubes.
7. The chilling tower for Fischer-Tropsch synthesis product separation of claim 1, wherein the spray washing system is provided in one or more layers, and comprises a liquid distribution pipe, and a plurality of liquid injection holes are formed in the middle lower part of the liquid distribution pipe.
8. The chilling tower for Fischer-Tropsch synthesis product separation according to claim 7, wherein the liquid distribution pipes are in a shark fin structure, the distribution pipes in two adjacent layers are arranged in a staggered manner, the liquid injection holes are uniformly distributed on two sides of the center line of the distribution pipes, the included angle of the liquid distribution pipes in two adjacent layers is 90 degrees,
the included angle of the central lines of the jet holes distributed on the two sides of the central line of the liquid distribution pipe is 20-140 degrees.
9. A quench tower for Fischer-Tropsch synthesis product separation according to claim 1, wherein the tray system comprises one or more layers of trays in the form of valve trays, valve trays or sieve trays, a liquid feed line is arranged above the trays, and the feed liquid is heavy oil, liquid light oil and filtered clean heavy oil liquid phase material at the bottom of the quench tower.
10. A quench tower for Fischer-Tropsch synthesis product separation according to claim 1, wherein a liquid-solid separation tank is further provided at the lower part of the liquid phase region of the quench tower body,
the liquid-solid separation tank comprises a bottom plate, a top plate, an outer partition plate and an inner partition plate, the bottom plate, the outer partition plate and a cylinder of the chilling tower form a liquid accumulation chamber with an opening at the upper part, and the lower part of the liquid accumulation chamber is connected with a liquid discharge hole;
the top plate, the inner partition plate and the barrel of the chilling tower form a cover body with an opening at the lower part, the cover body is arranged at the upper part of the liquid accumulation chamber, and a liquid flow passage with an inlet positioned at the bottom of the liquid accumulation chamber is formed between the inner partition plate and the outer partition plate.
11. A quench tower for fischer-tropsch synthesis product separation as recited in claim 10, wherein said inner and outer baffles are vertically disposed with a gap therebetween, and wherein said outer baffle has an upper portion spaced from said top plate, said top and bottom plates being welded to the wall of the tower using steel plates, said inner baffle being welded to the top plate, said outer baffle being welded to the bottom plate, the projection of said top plate being greater than the projection of the bottom plate, said top plate being disposed horizontally or obliquely.
12. A quench tower for the separation of products of the Fischer-Tropsch synthesis according to claim 10 or claim 11, wherein a pressure equalization tube is provided between the top of the liquid-solid separation tank and the gas phase zone of the quench tower.
13. A chilling tower for Fischer-Tropsch synthesis product separation according to claim 10, wherein one or more sets of liquid circulation systems are further provided, the liquid circulation systems comprise a circulation pipeline and a pressure raising pump, an inlet of the circulation pipeline is connected with a liquid phase region at the bottom of the chilling tower or a liquid discharge port of a liquid-solid separation tank, and an outlet of the circulation pipeline is connected with the spray washing system and/or the tray system.
14. A quench tower for Fischer-Tropsch synthesis product separation according to claim 1, wherein the quench tower is topped with a light oil discharge system comprising a mist eliminator and a discharge line, the mist eliminator being disposed inside the quench tower top.
15. A quench tower for Fischer-Tropsch synthesis product separation according to claim 1, wherein a heavy oil discharge system is arranged at the bottom of the quench tower, and comprises a heavy oil discharge port and pipeline, a flash tank, a filter, a storage tank and a booster pump.
16. A process system for Fischer-Tropsch synthesis product separation, which comprises the chilling tower of any one of claims 1 to 15, a flash tank, a filter, a heavy oil storage tank and a booster pump, and the specific process comprises the following steps:
gas-phase products from the top of the Fischer-Tropsch synthesis reactor enter a chilling tower through a main feeding system and an auxiliary feeding system, and light oil and reacted tail gas are sent to a post-process treatment through a tower top discharging system of the chilling tower in the form of gas-phase products;
and a part of the liquid phase heavy oil at the bottom of the chilling tower is sent to a liquid circulating system to be used as a washing liquid of a chilling tower spray washing system and/or a tower tray system, a part of the liquid phase heavy oil is extracted from the bottom of the tower to enter a tower bottom discharging system, light components are removed through a flash evaporation tank, solid particles are removed through a filter, the liquid phase heavy oil enters a heavy oil storage tank, the heavy oil is pressurized through a pressure raising pump and then is sent to a refining process, and/or a part of clean heavy oil is sent to the upper part of the chilling tower to be used as a washing liquid of.
17. The system of claim 16, wherein a raw gas from the fischer-tropsch synthesis reaction is used as a heat exchange medium to exchange heat with the light oil and tail gas from the top gas phase of the quench tower, and recover a portion of heat energy, and the recovered heat energy is sent to a heat exchanger at the lower portion of the quench tower to recover the heat energy of the heavy oil, and the preheated raw gas is sent to the fischer-tropsch synthesis reactor to react.
18. The process system for separating Fischer-Tropsch synthesis products of claim 16, wherein the temperature of the gas phase product feed of the Fischer-Tropsch synthesis reaction is 210-430 ℃, the operating pressure is 1.5-5.0 MPa, the temperature of the top of the chilling tower is 120-230 ℃, the temperature of the cooled heavy oil is 120-200 ℃, and the resistance of the chilling tower is less than 70 KPa.
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| CN118236850B (en) * | 2024-05-27 | 2024-07-30 | 山东东岳有机硅材料股份有限公司 | Process for the gas phase conversion of unsaturated hydrocarbons and chlorocarbons in chlorosilane reaction crudes |
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