CN104711006B - A kind of F- T synthesis system and method - Google Patents
A kind of F- T synthesis system and method Download PDFInfo
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- CN104711006B CN104711006B CN201510088925.0A CN201510088925A CN104711006B CN 104711006 B CN104711006 B CN 104711006B CN 201510088925 A CN201510088925 A CN 201510088925A CN 104711006 B CN104711006 B CN 104711006B
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- 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
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
- B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
-
- 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
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
- C10G2/34—Apparatus, reactors
- C10G2/342—Apparatus, reactors with moving solid catalysts
Abstract
The invention discloses a kind of F- T synthesis system and method, the F- T synthesis system includes paste state bed reactor, the first defecator, the first segregation apparatuss, the second segregation apparatuss and stripper；The present invention is by the cooperation of each device, catalyst fines that can be effectively in elimination reaction device, and catalyst fines are efficiently separated in can also realizing discharging product, and separation process design science, rationally, solve the problems, such as catalyst fines aggregation in paste state bed reactor, in synthetic product catalyst fines separate it is difficult, it is ensured that the continuous and steady operation of F- T synthesis system.
Description
Technical field
The present invention relates to F- T synthesis field, more particularly to a kind of F- T synthesis system based on paste state bed reactor
And method.
Background technology
With the increasingly reduction of petroleum resources, and the mankind, to the increasingly strict of requirement of preserving the ecological environment, the world is to clean
The demand of net liquid fuel is sharply increased, and in order to meet this demand, various countries' researcher is devoted to researching and developing clean combustion
The oily production technology of material, wherein being attracted most attention with Fischer-Tropsch (Fischer-Tropsch) synthetic technology.Typical fischer-tropsch synthesis process stream
Cheng Wei：First, the gasification of coal/natural gas Jing or partial oxidation, reforming for synthesis gas, then by synthetic gas desulfurization, deoxidizing purification
Afterwards, according to the fischer-tropsch synthesis process condition and catalyst for adopting, H/CO ratios are adjusted, is produced subsequently into Fischer-Tropsch synthesis device mixed
Close hydrocarbon.Finally, different target product is obtained after the separated processing modification of synthetic product.
Fischer-Tropsch synthesis device is the core reaction device for synthesizing oil tech, and the Fischer-Tropsch synthesis device reported has various shapes
Formula, including fixed bed, fluid bed and slurry bed system etc..As F- T synthesis paste state bed reactor has the uniform easily-controllable, gas of temperature fast
The advantages of opereating specification width, catalyst can be replaced online, therefore, current widely used the type reactor both at home and abroad.But,
In paste state bed reactor, the fluid product of synthesis has higher boiling point due to high molecular, it is not easy to vaporize, therefore generally
In liquid form in synthesis reactor inner accumulation, it is necessary to periodically or continuously which is discharged from inside reactor, so as to protect
The normal operation of card reactor.During de-waxing, in order to ensure high conversion, while avoiding catalyst loss, will need to be catalyzed
Agent fine powder is separated from synthetic wax product, allows its Returning reactor；Meanwhile, synthetic wax be processed further modify flow process
There are strict requirements to the content of solid catalyst.
In addition, for paste state bed reactor top discharge, on the one hand, in order to reduce in paste state bed reactor top discharge
Catalyst fines are carried secretly, it will usually which arranging on reactor top prevents the segregation apparatuss of Vapor Entrainment, by the catalyst in discharging
Fine grained and/or dust are separated with reactor head discharging so that this partial catalyst fine powder retains in the reactor, however,
This partial catalyst fine powder is due to damaged loss of catalytic activity already, and gathers in the reactor
Part filter load, it is serious when blocking filter element cause stop.On the other hand, even if being not provided with preventing gas phase on reactor top
The segregation apparatuss of entrainment, directly enter from the gaseous reaction products of reactor head out entrained catalyst fine grained and/or dust
Enter in subsequent separation system, and commonly use piece-rate system at present and be difficult to high efficiency separation be carried out to which.
United States Patent (USP) USP 3829478 discloses a kind of outer piece-rate system of typical slurry bed system.The system is from reactor
Serosity phase top draws the serosity containing catalyst outside reactor, then sends the gas phase isolated back to reaction by gas-liquid separation
Device, liquid phase enter serosity settling tank；In settling tank, catalyst granules is by gravitational settling to bottom；Bottom is rich in catalyst
The serum recycle Returning reactor of granule, top are substantially free of the liquid of catalyst granules and are drawn by settling tank top.The method
The separation of catalyst granules and fluid product is realized mainly by gravitational settling, therefore infall process is longer, and sedimentation point
It is larger from tank size.Patent WO02/96840 A1 discloses a kind of magnetic separator, sets up on the outside of the outer circulation main pipeline of serosity
T-shaped Magnet.When the slurry stream containing catalyst is out-of-date, partial catalyst granule is adsorbed onto on tube wall by magnetic field so that from arm
In the serosity of outflow, catalyst concn is accordingly reduced, and this fraction slurries enters back into the defecator in downstream and isolates heavy hydrocarbon.Should
Method can mitigate the operational load of defecator to a certain extent, but equipment is relative complex, and the outer circulation main pipeline of serosity
There is certain difficulty in the recovery of institute's adsorption catalyst, utilization on wall.
Therefore, in order to maintain the normal operation of Fischer-Tropsch synthesis system, loss and the elimination reaction device gas of catalyst are reduced
Mutually catalyst fines in discharging and liquid phase discharging, develop continuous effective, economical rationality solid- liquid separation technology for
It is very necessary for the industrialization target of syrup state bed Fischer Tropsch synthesis.
The content of the invention
It is an object of the invention to provide a kind of F- T synthesis system and method, is gone out with the gas phase for solving paste state bed reactor
Expect the problem of difficulty is separated with catalyst in liquid phase discharging, it is ensured that the continuous and steady operation of F- T synthesis system.
For achieving the above object in a first aspect, the present invention is employed the following technical solutions：
A kind of F- T synthesis system, the F- T synthesis system include：
Paste state bed reactor, for carrying out Fischer-Tropsch synthesis；
First defecator, first defecator are arranged in the paste state bed reactor, draw institute for treating
The catalyst stated in the liquid phase discharging of paste state bed reactor is filtered；
First segregation apparatuss, for carrying out gas-liquid separation to the filtrate from first defecator, to obtain gas phase
Product and liquid product；
Second segregation apparatuss, for carrying out gas-liquid separation to the gas phase discharging from the paste state bed reactor, to obtain
Gas-phase product and liquid product；With
Stripper, for the gas-phase product and liquid product from first segregation apparatuss, and from described
The liquid product of two segregation apparatuss carries out stripping separation, wherein, tower top discharging opening, bottom are provided with the top of the stripper and are provided with
Bottom of towe discharging opening；Between the tower top discharging opening and bottom of towe discharging opening, the stripper is from top to bottom additionally provided with the second separation
Device fluid inlet, product exit, the first segregation apparatuss fluid inlet, the first segregation apparatuss gas phase import and steam inlet；Institute
Steam inlet is stated for receiving Stripping Steam, the product exit is used to discharge grade product.
F- T synthesis system of the invention, it is preferable that second segregation apparatuss include：
First separator, for carrying out gas-liquid separation to the gas phase discharging from the paste state bed reactor；Described first
Heat exchange coil is provided with separator, the heat exchange coil is used to make the gas phase from the paste state bed reactor discharge and wait to enter
The unstripped gas heat exchange condensation of the paste state bed reactor；
First condenser, for condensing to the gas-phase product from first separator；
Second separator, for carrying out gas-liquid separation to the condensed product of first condenser；
3rd separator, for carrying out decompression separation to the liquid product from the second separator；3rd separator
For horizontal tank body separator, the threeth separator overflow plate for extending is provided with from its bottom up in the 3rd separator, from
And the 3rd separator is divided into positioned at the feed zone of the 3rd separator overflow plate side and positioned at the 3rd separation
The overflow area of device overflow plate opposite side；The 3rd separator feed pipe, bottom are provided with the top of the 3rd separator feed zone to set
There is the 3rd separator drain pipe, the 3rd separator gaseous phase outlet pipe, bottom are provided with the top of the 3rd separator overflow area and are set
There is the 3rd separator liquid-phase outlet pipe, for discharging isolated liquid product；
The stripper is received from first separator and the 3rd point by the second segregation apparatuss fluid inlet
From the liquid product of device.Preferably, the second segregation apparatuss fluid inlet is provided with two along longitudinal direction on the stripper, its
In, position is used to receive the liquid product from the 3rd separator in the second upper segregation apparatuss fluid inlet, and position exists
Under the second segregation apparatuss fluid inlet be used for receive from first separator liquid product.The present invention is more by arranging
Individual separator carries out multiple stage separation, not only allows gas-phase product effectively Removal of catalyst fine powder, while so that first separates
Can still keep higher temperature in device, and the temperature in later separation device need to only accordingly reduced, it is to avoid adopt single separation
Need material is all reduced to the situation of relevant temperature during device, be conducive to energy-conservation and follow-up stripping.
F- T synthesis system of the invention, it is preferable that first defecator includes at least one filtration pipe fitting,
The filtration pipe fitting includes outer filter tube, interior filter tube, outer discharge nozzle and interior discharge nozzle, and the interior filter tube is arranged on described outer
Inside filter tube, and the filter opening diameter of the interior filter tube is less than the filter opening diameter of the outer filter tube；The outer filter tube
Top be provided with outer backwash mouth, for counter-flushing liquid is introduced into the outer filter tube, the top of the interior filter tube is provided with
Interior backwash mouth, for introducing counter-flushing liquid into the interior filter tube；The outer discharge nozzle is connected to the outer filter tube
Bottom, for the filtration product drawn between the outer filter tube and interior filter tube and sends the paste state bed reactor back to；It is described
Interior discharge nozzle is connected to the bottom of the interior filter tube, for drawing the filtration product in the interior filter tube.The mistake of the present invention
Chimney filter part is longitudinally arranged at the middle part of reactor, can reduce the obstruction to pulp flow in reactor, while longitudinal flow
Slurry effectively can also remove filter pipe fitting surface attachment solid obstruction thing, improve filter efficiency.
F- T synthesis system of the invention, it is preferable that the outer filter tube is provided with non-filtered section, the non-filtered
Section is located at the bottom of the outer filter tube, such as the of length no more than described outer of described non-filtered section filters the 1/2 of length of tube, institute
Interior filter tube is stated in the non-filtered section, this product that can be designed so that the outer filter tube filtrations of Jing are entered will not
The surface of the interior filter tube is directly acted in the presence of inertia, but is flowed downward, in the bottom of the outer filter tube
Contact with the interior filter tube, as product is parallel with the filtering surface of the interior filter tube, institute is attached to so as to take away
The interior catalyst granules for filtering pipe surface is stated, it is unimpeded to help to maintain filter opening, improve filter efficiency.
F- T synthesis system of the invention, it is preferable that a diameter of 15-60 microns of filter opening of the outer filter tube, opens
Porosity is not less than 30%, and a diameter of 1-10 microns of filter opening of the interior filter tube, percent opening are not less than 60%, the outer filter tube
Diameter interior filter 1.5 times of pipe diameter not less than described；It is further preferred that a diameter of 20- of filter opening of the outer filter tube
50 microns, percent opening is not less than 35%；The a diameter of 2-8 microns of filter opening of the interior filter tube, percent opening are not less than 65%, described
1.5-3 times of a diameter of described interior filtration pipe diameter of outer filter tube；It is further preferred that the filter opening of the outer filter tube is straight
Footpath is 30-40 microns, and percent opening is 40-50%；The a diameter of 4-6 microns of filter opening of the interior filter tube, percent opening is 70-
80%, 1.8-2.5 times of a diameter of described interior filtration pipe diameter of the outer filter tube.
It is further preferred that first defecator is provided with multigroup, such as 3-12 groups or 5-8 groups, in sustained height
On be evenly arranged around paste state bed reactor side wall, every group of defecator includes 3-30 roots, preferred 5-25 roots, more preferably 10-
20 filtration pipe fittings, to improve filtering rate.
F- T synthesis system of the invention, it is preferable that the paste state bed reactor be additionally provided with gas distributor, first
Heat exchanger and the second heat exchanger, the gas distributor are built in the paste state bed reactor bottom, and the First Heat Exchanger sets
It is placed in the paste state bed reactor and is located on first defecator, second heat exchanger is arranged on the slurry
Outside state bed reactor, and pass through slurry effuser and slurry inflow pipe and paste state bed reactor formation heat-exchanging loop, wherein,
One end of the slurry effuser is connected to position of the paste state bed reactor below the first defecator, the slurry
The other end of effuser is connected to the charging aperture on the second heat exchanger top；One end of the slurry inflow pipe is connected to described
Paste state bed reactor is located at the position between the slurry effuser and gas distributor, and the slurry flows into the other end of pipe and connects
It is connected to the discharging opening of the second heat exchanger bottom.
F- T synthesis system of the invention, it is preferable that the F- T synthesis system also includes the 3rd segregation apparatuss, institute
Stating the 3rd segregation apparatuss includes：
Second condenser, condenses for the tower top discharging to the stripper；With
4th separator, for separating to the condensed product from second condenser；4th separator
For horizontal tank body separator, the fourth separator overflow plate for extending is provided with from its bottom up in the 4th separator, from
And the 4th separator is divided into positioned at the feed zone of the 4th separator overflow plate side and positioned at the 4th separation
The overflow area of device overflow plate opposite side；The 4th separator feed pipe, bottom are provided with the top of the 4th separator feed zone to set
There is the 4th separator drain pipe, the 4th separator gaseous phase outlet pipe, bottom are provided with the top of the 4th separator overflow area and are set
There is the 4th separator liquid-phase outlet pipe, for discharging grade product.
F- T synthesis system of the invention, it is preferable that the F- T synthesis system also includes the second defecator, institute
Stating the second defecator includes：
First filter, filters for the bottom of towe discharging to the stripper；
Desorption tank, the filtrate for making first filter are sufficiently mixed with filter aid；With
Second filter, for filtering to the material from the desorption tank, obtains grade product.
F- T synthesis system of the invention, it is preferable that the F- T synthesis system also includes decarburization unit, for taking off
Except the carbon dioxide in the gas-phase product of second separator, the 3rd separator and the 4th separator, and by the gas after decarburization
Body sends the paste state bed reactor back to as unstripped gas, so that the liquid and gas discharging of paste state bed reactor can be obtained
Process, utilize to rational.
Second aspect for achieving the above object, the present invention are employed the following technical solutions：
A kind of method for carrying out F- T synthesis using above-mentioned F- T synthesis system, methods described are included using the slurry
Bed reactor carries out F- T synthesis；Treated using the first defecator draw the paste state bed reactor liquid phase discharging carried out
Filter；Gas-liquid separation is carried out to the filtrate from first defecator using first segregation apparatuss, to obtain gas phase product
Thing and liquid product；Gas-liquid point is carried out to the gas phase discharging from the paste state bed reactor using second segregation apparatuss
From；With in the presence of vapor, the gas-phase product from first segregation apparatuss and liquid phase are produced using the stripper
Thing, and carry out stripping separation from the liquid product of second segregation apparatuss, and discharged by the product exit it is qualified
Product.
Method in accordance with the invention it is preferred that methods described is also included using the 3rd segregation apparatuss to the stripping
The tower top discharging of tower is separated, and discharges synthetic product by the 4th separator liquid-phase outlet pipeline；Using described
Bottom of towe discharging of two defecators to the stripper is filtered, and obtains grade product by the second filter；And utilization
Titanium dioxide of the decarburization unit removing in the gas-phase product of second separator, the 3rd separator and the 4th separator
Carbon, and the gas after decarburization is sent back to the paste state bed reactor as unstripped gas.
Method in accordance with the invention it is preferred that the charging solid content of first segregation apparatuss is not more than 60ppm；It is described
The bottom of towe discharging flow of stripper is 0.3-0.5 times of the liquid phase feeding flow of the stripper, and solid content is described first to separate
2-3.8 times of device charging solid content, wherein, the flow is volume flow.It is further preferred that first segregation apparatuss
Charging solid content be not more than 50ppm；The bottom of towe discharging flow of the stripper is the liquid phase feeding flow of the stripper
0.35-0.45 times, solid content is 2.3-3.4 times of the first segregation apparatuss charging solid content.
The F- T synthesis system of the present invention, discharges for the liquid phase of paste state bed reactor, by the first defecator to thing
Material carries out pre-separation, due to allowing have certain solid content (such as being not more than 60ppm) in filtrate, so as to be conducive to from described
In paste state bed reactor Removal of catalyst fine grained and keep compared with filtration efficiency；Also, from the filtrate of the first defecator
Stripper is respectively fed to Jing after the first segregation apparatuss are separated into gas-liquid two-phase, stripper load is advantageously reduced, stripping effect is improved
Really.Discharge for the gas phase of paste state bed reactor, without the need for arranging gas-tight phase entrainment device again, be conducive to from paste state bed reactor
Removal of catalyst fine grained, is separated by gas phase discharging of second segregation apparatuss to paste state bed reactor, makes gas phase discharge
The catalyst fines (or catalyst fines) of middle entrainment are primarily entered in the liquid phase that the second segregation apparatuss are isolated, to send into
Stripper is focused on, and simplifies piece-rate system.In addition, Jing after stripper is separated, can obtain no less than stripper liquid phase feeding
The grade product of flow 30%, can equally obtain grade product, and bottom of towe discharging can then be concentrated after tower top discharging is separated
Most solid phase particles, although its solid concentration is high, but flow reduction, are very suitable for filtration treatment in subsequent set, and nothing
Main equipment is needed, filter efficiency is high.Therefore, by the cooperation of each device, the present invention realizes that product is separated, separation process design department
Learn, rationally, solve catalyst fines aggregation in paste state bed reactor, and in synthetic product catalyst fines separate it is difficult
Problem, it is ensured that continuous, the stable operation of F- T synthesis system.
Description of the drawings
Fig. 1 is the structural representation of the F- T synthesis system of the present invention；
Schematic diagrams of the Fig. 2 for a kind of embodiment of filtration pipe fitting in the first defecator in Fig. 1；
Fig. 3 is a kind of structural representation of embodiment of paste state bed reactor in Fig. 1.
Specific embodiment
Below in conjunction with accompanying drawing, the present invention is described in detail, but the present invention is not limited only to this.
As shown in figure 1, the F- T synthesis system of paste state bed reactor that the present invention is provided include paste state bed reactor 1, the
One defecator 2, the first segregation apparatuss 3, the second segregation apparatuss 4 and stripper 5.
Wherein, first defecator 2 is arranged in the paste state bed reactor 1, draws the slurry for treating
Catalyst in the liquid phase discharging of bed reactor 1 is filtered, to reduce the bulky grain that people in liquid phase discharging has catalysis activity
The content of catalyst.In a preferred embodiment, as shown in Fig. 2 first defecator 2 includes one or more mistakes
Chimney filter part 9, the filtration pipe fitting 9 include outer filter tube 91, interior filter tube 92, outer discharge nozzle 93 and interior discharge nozzle 94, described interior
Filter tube 92 is arranged on inside the outer filter tube 91, and the filter opening diameter of the interior filter tube 92 is less than the outer filtration
The filter opening diameter of pipe 91；The top of the outer filter tube 91 is provided with outer backwash mouth 911, for drawing into the outer filter tube 91
Enter counter-flushing liquid, the top of the interior filter tube 92 is provided with interior backwash mouth 921, for introducing anti-into the interior filter tube 92
Flushing liquor；The outer discharge nozzle 93 is connected to the bottom of the outer filter tube 91, for drawing the outer filter tube 91 and interior mistake
Filtration product between chimney filter 92；The interior discharge nozzle 94 is connected to the bottom of the interior filter tube 92, for drawing in described
Filtration product in filter tube 92.
In a preferred embodiment, a diameter of 15-60 microns of the filter opening of the outer filter tube 91, percent opening are not less than
30%, a diameter of 1-10 microns of filter opening of the interior filter tube 92, percent opening are not less than 60%, the diameter of the outer filter tube 91
Not less than 1.5 times of 92 diameter of interior filter tube；It is further preferred that a diameter of 20-50 of filter opening of the outer filter tube 91
Micron, percent opening are not less than 35%；The a diameter of 2-8 microns of filter opening of the interior filter tube 92, percent opening are not less than 65%, described
1.5-3 times of a diameter of described 92 diameter of interior filter tube of outer filter tube 91；It is further preferred that the outer filter tube 91
The a diameter of 30-40 microns of filter opening, percent opening is 40-50%；The a diameter of 4-6 microns of filter opening of the interior filter tube 92, percent opening
For 70-80%, 1.8-2.5 times of a diameter of described 92 diameter of interior filter tube of the outer filter tube 91.
In the present invention, after Fischer-Tropsch synthetic to be separated 91 filtering and removing of the outer filter tube major part catalyst described in
Into in outer filter tube 91, the larger catalyst of 92 filtering and removing of interior filter tube described in further Jing in the outer filter tube 91
After granule, described in Jing, interior discharge nozzle 94 is drawn, and is gone out between the outer filter tube 91 and interior filter tube 92 described in remaining material Jing
Expects pipe 93 is drawn, and can be further fed into storage tank or send the paste state bed reactor 1 back to.By double-filtration, effectively can prevent
Only filter opening obstruction, improves filter efficiency, is particularly suitable for the filtration of the larger Fischer-Tropsch synthetic of viscosity of the invention.In addition,
The filtration pipe fitting 9 of the present invention can also utilize the outer backwash mouth 911 and interior backwash mouth 921 periodically to introduce flushing liquor to institute
Stating outer filter tube 91 and interior filter tube 92 carries out backwash, to reduce filtration resistance.
In a preferred embodiment of the filtration pipe fitting 9 of the present invention, the outer filter tube 91 is provided with non-filtered section 912
(being not provided with the part of filter opening), the non-filtered section 912 are located at the bottom of the outer filter tube 91, the interior filter tube 92
In the non-filtered section 912.This product that can be designed so that the outer filtrations of filter tube 91 of Jing are entered will not be in inertia
In the presence of directly act on the surface of the interior filter tube 92, but flow downward, the bottom of the outer filter tube 91 with
The interior filter tube 92 is contacted, due to the flow direction of product it is parallel with the filtering surface of the interior filter tube 92, so as to
The catalyst granules for being attached to 92 surface of interior filter tube can be taken away, it is unimpeded to help to maintain filter opening, improve filter efficiency.
It will be understood by those skilled in the art that in order to improve filter efficiency, first defecator can be provided with multigroup,
Such as 3-12 groups or 5-8 groups, are evenly arranged around 1 side wall of the paste state bed reactor on sustained height, per group first filtration
Device is provided with 3-30 roots, and preferred 5-25 roots, more preferably 10-20 roots filter pipe fitting, to improve filtering rate.
The paste state bed reactor 1 is used to carry out Fischer-Tropsch synthesis, and which can be slurry reactor commonly used in the art
One of device.In a preferred embodiment of the invention, as shown in figure 3, the paste state bed reactor 1 is additionally provided with gas distributor
12nd, First Heat Exchanger 13 and the second heat exchanger 14, the gas distributor 12 are built in 1 bottom of the paste state bed reactor, with
The unstripped gas of entrance is made to be evenly distributed.The First Heat Exchanger 13 is arranged in the paste state bed reactor 1 and is located at described
On first defecator 2, second heat exchanger 14 is arranged on outside the paste state bed reactor 1, and passes through slurry effuser
15 and slurry flow into pipe 16 and the paste state bed reactor 1 and form heat-exchanging loop, wherein, one end of the slurry effuser 15 connects
It is connected to position of the paste state bed reactor 1 below the first defecator 2, the other end connection of the slurry effuser 15
To the charging aperture on 14 top of the second heat exchanger；The slurry flows into one end of pipe 16 and is connected to the paste state bed reactor 1
Position between the slurry effuser 15 and gas distributor 12, the slurry flow into the other end of pipe 16 and are connected to institute
State the discharging opening of 14 bottom of the second heat exchanger.
In reactor lower part, as fresh feed gas is contacted with catalyst, its reaction is compared with the middle part of reactor and top more
Acutely, by reactor lower part serosity is sent into heat exchange cooling in the second external heat exchanger 14, and make the slurry of reactor lower part
Material is circulated, and can improve heat exchange efficiency, and is conducive to the uniform contact of gas and catalyst, improves reaction efficiency；
In the middle part of reactor and top reacts more gentle, and the heat of accumulation can be changed be arranged on reactor top first by serosity
The contact of hot device 13 is removed, and improves the space availability ratio of paste state bed reactor 1, meanwhile, the slurry Jing after First Heat Exchanger 13 is lowered the temperature
Liquid is increased due to density, can be backflowed further downward, so as to be conducive to the uniform contact of gas and catalyst, improves reaction effect
Rate.
First segregation apparatuss 3 for carrying out gas-liquid separation to the filtrate from first defecator 2, to obtain
Gas-phase product and liquid product.It will be understood by those skilled in the art that first segregation apparatuss 3 can include one or more
Gas-liquid separator, for example, first segregation apparatuss 3 include two gas-liquid separators, and one of them is for from described
The filtrate of one defecator 2 carries out gas-liquid separation, and another carries out gas-liquid point for the gas-phase product to previous gas-liquid separator
From.
Second segregation apparatuss 4 carry out gas-liquid separation for discharging to the gas phase from the paste state bed reactor 1, with
Obtain gas-phase product and liquid product.
The stripper 5 for the gas-phase product and liquid product from first segregation apparatuss 3, and from institute
The liquid product for stating the second segregation apparatuss 4 carries out stripping separation, wherein, the top of the stripper 5 is provided with tower top discharging opening (figure
In do not mark), bottom be provided with bottom of towe discharging opening (not marking in figure)；Between the tower top discharging opening and bottom of towe discharging opening, institute
State stripper 5 and be from top to bottom additionally provided with and (scheme for the second segregation apparatuss fluid inlet for receiving 4 liquid product of the second segregation apparatuss
In do not mark), product exit (not marking in figure), for receive 3 liquid product of the first segregation apparatuss the first segregation apparatuss liquid
Phase import (not marking in figure), for receive 3 gas-phase product of the first segregation apparatuss the first segregation apparatuss gas phase import (in figure not
Mark) and steam inlet (not marking in figure)；The steam inlet is used to receive Stripping Steam, and the product exit is used to arrange
(i.e. catalyst removal amount reaches the Fischer-Tropsch synthetic of requirement, hereinafter referred to as qualified to go out the qualified Fischer-Tropsch synthetic of solid content
Product), for example solid content is less than 2ppm.
In one preferred embodiment, second segregation apparatuss 4 include the first separator 41, the first condenser
42nd, the second separator 43 and the 3rd separator 44.Wherein, first separator 41 is for from the paste state bed reactor
1 gas phase discharging carries out gas-liquid separation；Heat exchange coil is provided with first separator, the heat exchange coil is used to make from institute
State the gas phase discharging of paste state bed reactor 1 and treat the unstripped gas heat exchange condensation into the paste state bed reactor 1.Described first is cold
Condenser 42 is for condensing to the gas-phase product from first separator 41；Second separator 43 is for described
The condensed product of the first condenser 42 carries out gas-liquid separation.
3rd separator 44 for carrying out decompression separation to the liquid product from the second separator 43, the described 3rd
Separator 44 is horizontal tank body separator, and the 3rd separator for extending is provided with from its bottom up in the 3rd separator 44
Overflow plate 45, so as to 44 points is positioned at feed zone and the position of 45 side of the 3rd separator overflow plate by the 3rd separator
In the overflow area of 45 opposite side of the 3rd separator overflow plate；The 3rd separation is provided with the top of the 3rd separator feed zone
Device feed pipe 46, bottom is provided with the 3rd separator drain pipe 47, is provided with the 3rd separation at the top of the 3rd separator overflow area
Device gaseous phase outlet pipe 48, bottom is provided with the 3rd separator liquid-phase outlet pipe 49, for discharging isolated liquid product.It is described
Stripper 5 is received from first separator 41 and the liquid of the 3rd separator 44 by the second segregation apparatuss fluid inlet
Phase product.Preferably, the second segregation apparatuss fluid inlet is provided with two along longitudinal direction on the stripper 5, wherein, position
It is used to receive the liquid product from the 3rd separator 44, position under the in the second upper segregation apparatuss fluid inlet
Two segregation apparatuss fluid inlets are used to receive the liquid product from first separator 41.
In a preferred embodiment of the present invention, the F- T synthesis system also includes the second defecator the 6, the 3rd
Segregation apparatuss 7 and decarburization unit 8.Second defecator 6 includes the first filter 61, desorption tank 62 and the second filter
63, first filter 61 is filtered for the bottom of towe discharging to the stripper 4；The desorption tank 62 is described for making
The filtrate of the first filter 61 is sufficiently mixed with filter aid；Second filter 63 is for the thing from the desorption tank 62
Material is filtered, and obtains grade product.
3rd segregation apparatuss 7 include the second condenser 71 and the 4th separator 72, and second condenser 71 is used for
Tower top discharging to the stripper 4 is condensed；4th separator 72 is for the condensation from the condenser 71
Product is separated；4th separator 72 is horizontal tank body separator, is provided with from its bottom in the 4th separator 72
The upwardly extending 4th separator overflow plate 73 in portion, so as to the 4th separator is divided into positioned at the 4th separator overflow
The feed zone of plate side and the overflow area positioned at the 4th separator overflow plate opposite side；The 4th separator feed zone
Top is provided with the 4th separator feed pipe 74, bottom and is provided with the 4th separator drain pipe 75, the 4th separator overflow area
Top is provided with the 4th separator gaseous phase outlet pipe 76, bottom and is provided with the 4th separator liquid-phase outlet pipe 77, for discharging qualified product
Thing；In one embodiment, portion of product and the 3rd in the grade product that the 4th separator liquid-phase outlet pipe 77 is discharged
The liquid product of separator 44 together sends into stripper 5, to increase overhead reflux.
The decarburization unit 8 is used for removing from second separator 43, the 3rd separator 44 and the 4th separator 72
Gas-phase product in carbon dioxide, and send the gas after carbon dioxide removal back to the paste state bed reactor as unstripped gas
1.The decarburization unit 8 is known in the art, and for example, in one embodiment, the decarburization unit 8 can include water scrubber
And caustic wash tower, after gas-phase product washs oxygen-bearing organic matter first in water scrubber, then after exchanging heat, temperature rises to 80 DEG C～95 DEG C, enters
Enter caustic wash tower bottom of towe, carbon dioxide removal, in making tower top outlet purified gas, carbon dioxide content drops to about less than 2.0%；One
Plant in embodiment, from one of the gas-phase product of second separator 43, the 3rd separator 44 and the 4th separator 72
Divide and can process without the decarburization unit 8 and paste state bed reactor 1 be returned directly as unstripped gas, with unstripped gas is met
On the premise of carbon dioxide content is required, reduce the load of the decarburization unit 8.
During operation, the filtrate from first defecator 2 carries out gas-liquid separation into first segregation apparatuss 3,
Gas phase discharging from the paste state bed reactor 1 and treats the unstripped gas into paste state bed reactor 1 into the first separator 41
Heat exchange cooling, to realize gas-liquid separation, the gas phase that the first separator 41 is isolated enters second Jing after the condensation of the first condenser 42
Separator 43 carries out gas-liquid separation, and the second separator 43 is isolated liquid phase and is further fed into the 3rd separator 44 and carries out decompression point
From the gas phase isolated is discharged from the 3rd separator gaseous phase outlet pipe 49, and water is discharged from the 3rd separator drain pipe 47, overflow
Liquid phase is discharged from the 3rd separator liquid-phase outlet pipe 48.
Stripper 5 receives the gas-phase product from the first segregation apparatuss 2 by the first segregation apparatuss gas phase import, by the
One segregation apparatuss fluid inlet receives the liquid product from the first segregation apparatuss 2, is connect by the second segregation apparatuss fluid inlet
Receive from the first separator 41 and the liquid product of the 3rd separator 44.Vapor Jing steam inlets used by stripping enter stripper
5 are stripped, and after stripping, grade product Jing product exits are discharged.5 tower top of stripper goes out material into the 3rd segregation apparatuss 7, Jing
Second condenser 71 is entered in the 4th separator 72 after condensing and is separated, and water discharges 75 from the 4th separator drain pipe, and gas phase is from the
Four separator gaseous phase outlet pipes 76 are discharged, and grade product is discharged from the 4th separator liquid-phase outlet pipe 77.The low discharging of 5 tower of stripper
Into the second defecator 6, Jing after the first filter 61 is filtered, desorption tank 62 by filter aid (such as hargil and kieselguhr) with
The filtrate of the first filter 61 is sufficiently mixed, and with the molecule in absorption filtrate, is then filtered by the second filter 63
To grade product.Send into from the gas-phase product of second separator 43, the 3rd separator 44 and the 4th separator 72 described
To remove the carbon dioxide in gas phase, the gas after decarburization returns the paste state bed reactor 1 as unstripped gas to decarburization unit 8.
The present invention also provides a kind of method for carrying out F- T synthesis using above-mentioned F- T synthesis system, and methods described includes profit
Fischer-Tropsch synthesis are carried out with the paste state bed reactor 1, the extraction paste state bed reactor are treated using the first defecator 2
1 liquid phase discharging is filtered；Enter circulation of qi promoting using first segregation apparatuss, 3 pairs of filtrates from first defecator 2
Liquid is separated, to obtain gas-phase product and liquid product；Using second segregation apparatuss 4 pairs from the paste state bed reactor 1
Gas phase discharging carry out gas-liquid separation；With in the presence of vapor, using the stripper, 5 pairs separate dress from described first
Put 3 gas-phase product and liquid product, and stripping separation is carried out from the liquid product of second segregation apparatuss 4, and lead to
Cross the product exit and discharge grade product.
In a preferred embodiment, methods described is also included using described 3rd segregation apparatuss, 7 pairs of strippers 5
Tower top discharging separated, and grade product is discharged by the liquid-phase outlet pipe 77 of the separator 72；Using described second
The bottom of towe discharging of 6 pairs of strippers 4 of defecator is filtered, and is filtrated to get grade product by the second filter 63；
With the gas phase from second separator 43, the 3rd separator 44 and the 4th separator 72 is removed using the decarburization unit 8
Carbon dioxide in product, and the gas after decarburization is sent back to the paste state bed reactor 1 as unstripped gas.
In a preferred embodiment of the present invention, the charging solid content of first segregation apparatuss 3 is not more than
60ppm；The bottom of towe discharging flow of the stripper 5 is 0.3-0.5 times of the liquid phase feeding flow of the stripper 5, and solid content is
2-3.8 times of the charging of first segregation apparatuss 3 solid content, wherein, the flow is volume flow.It is further preferred that institute
The charging solid content for stating the first segregation apparatuss 3 is not more than 50ppm；The bottom of towe discharging flow of the stripper 5 is the stripper 5
0.35-0.45 times of liquid phase feeding flow, solid content is 2.3-3.4 times of first segregation apparatuss 3 charging solid content.
Claims (11)
1. a kind of F- T synthesis system, the F- T synthesis system include：
Paste state bed reactor, for carrying out Fischer-Tropsch synthesis；
First defecator, first defecator are arranged in the paste state bed reactor, draw the slurry for treating
Catalyst in the liquid phase discharging of state bed reactor is filtered；
First segregation apparatuss, for carrying out gas-liquid separation to the filtrate from first defecator, to obtain gas-phase product
And liquid product；
Second segregation apparatuss, for carrying out gas-liquid separation to the gas phase discharging from the paste state bed reactor, to obtain gas phase
Product and liquid product；With
Stripper, for the gas-phase product and liquid product from first segregation apparatuss, and from described second point
Liquid product from device carries out stripping separation, wherein, tower top discharging opening, bottom are provided with the top of the stripper and are provided with bottom of towe
Discharging opening；Between the tower top discharging opening and bottom of towe discharging opening, the stripper is from top to bottom additionally provided with the second segregation apparatuss
Fluid inlet, product exit, the first segregation apparatuss fluid inlet, the first segregation apparatuss gas phase import and steam inlet；The steaming
Vapour entrance is used to receive Stripping Steam, and the product exit is used to discharge grade product；
Wherein, first defecator includes at least one filtration pipe fitting, and the filtration pipe fitting includes outer filter tube, interior filtration
Pipe, outer discharge nozzle and interior discharge nozzle, the interior filter tube is arranged on inside the outer filter tube, and the filter of the interior filter tube
Filter opening diameter of the bore dia less than the outer filter tube；The top of the outer filter tube is provided with outer backwash mouth, for described
Counter-flushing liquid is introduced in outer filter tube, the top of the interior filter tube is provided with interior backwash mouth, for into the interior filter tube
Introduce counter-flushing liquid；The outer discharge nozzle is connected to the bottom of the outer filter tube, for drawing the outer filter tube and interior mistake
Filtration product between chimney filter simultaneously sends the paste state bed reactor back to；The interior discharge nozzle is connected to the bottom of the interior filter tube
Portion, for drawing the filtration product in the interior filter tube；
The paste state bed reactor is additionally provided with gas distributor, and the gas distributor is built under the paste state bed reactor
Portion, so that the unstripped gas for entering is evenly distributed.
2. F- T synthesis system according to claim 1, it is characterised in that second segregation apparatuss include：
First separator, for carrying out gas-liquid separation to the gas phase discharging from the paste state bed reactor；Described first separates
It is provided with heat exchange coil in device, the heat exchange coil is used to making gas phase discharging from the paste state bed reactor and treats into described
The unstripped gas heat exchange condensation of paste state bed reactor；
First condenser, for condensing to the gas-phase product from first separator；
Second separator, for carrying out gas-liquid separation to the condensed product of first condenser；
3rd separator, for carrying out decompression separation to the liquid product from the second separator；3rd separator is sleeping
Formula tank body separator, is provided with from its bottom up in the 3rd separator the 3rd separator overflow plate for extending, so as to incite somebody to action
3rd separator is divided into positioned at the feed zone of the 3rd separator overflow plate side and overflows positioned at the 3rd separator
The overflow area of stream plate opposite side；The 3rd separator feed pipe, bottom are provided with the top of the 3rd separator feed zone and are provided with
Three separator drain pipies, are provided with the 3rd separator gaseous phase outlet pipe, bottom and are provided with the top of the 3rd separator overflow area
Three separator liquid-phase outlet pipes, for discharging isolated liquid product；
The stripper is received from first separator and the 3rd separator by the second segregation apparatuss fluid inlet
Liquid product.
3. F- T synthesis system according to claim 2, it is characterised in that the outer filter tube is provided with non-filtered section,
The non-filtered section is located at the bottom of the outer filter tube, and the interior filter tube is located in the non-filtered section.
4. F- T synthesis system according to claim 3, it is characterised in that first defecator is provided with 3-12 groups,
On sustained height, around the paste state bed reactor side, wall is evenly arranged, and every group of defecator includes that 3-30 roots filter pipe fitting.
5. F- T synthesis system according to claim 3, it is characterised in that a diameter of 15- of filter opening of the outer filter tube
60 microns, percent opening is not less than 30%, and a diameter of 1-10 microns of filter opening of the interior filter tube, percent opening are not less than 60%, institute
State a diameter of described interior filter pipe diameter 1.5-3 times of outer filter tube.
6. F- T synthesis system according to claim 1, it is characterised in that the F- T synthesis system also includes the second mistake
Filter device, second defecator include：
First filter, filters for the bottom of towe discharging to the stripper；
Desorption tank, the filtrate for making first filter are sufficiently mixed with filter aid；With
Second filter, for filtering to the material from the desorption tank, obtains grade product.
7. the F- T synthesis system according to any one of claim 2-5, it is characterised in that the F- T synthesis system is also
Including the 3rd segregation apparatuss, the 3rd segregation apparatuss include：
Second condenser, condenses for the tower top discharging to the stripper；With
4th separator, for separating to the condensed product from second condenser；4th separator is sleeping
Formula tank body separator, is provided with from its bottom up in the 4th separator the 4th separator overflow plate for extending, so as to incite somebody to action
4th separator is divided into positioned at the feed zone of the 4th separator overflow plate side and overflows positioned at the 4th separator
The overflow area of stream plate opposite side；The 4th separator feed pipe, bottom are provided with the top of the 4th separator feed zone and are provided with
Four separator drain pipies, are provided with the 4th separator gaseous phase outlet pipe, bottom and are provided with the top of the 4th separator overflow area
Four separator liquid-phase outlet pipes, for discharging isolated grade product.
8. F- T synthesis system according to claim 7, it is characterised in that the F- T synthesis system also includes decarburization list
Unit, for removing the carbon dioxide in the gas-phase product of second separator, the 3rd separator and the 4th separator, and will be de-
Gas after carbon sends the paste state bed reactor back to as unstripped gas.
9. F- T synthesis system according to claim 3, it is characterised in that the paste state bed reactor is additionally provided with first and changes
Hot device and the second heat exchanger, the First Heat Exchanger are arranged in the paste state bed reactor and filter dress positioned at described first
On putting, second heat exchanger is arranged on outside the paste state bed reactor, and pass through slurry effuser and slurry flow into pipe with
The paste state bed reactor forms heat-exchanging loop, wherein, one end of the slurry effuser is connected to the paste state bed reactor
Position below the first defecator, the other end of the slurry effuser are connected to entering for the second heat exchanger top
Material mouth；The slurry flows into one end of pipe and is connected to the paste state bed reactor positioned at the slurry effuser and gas distributor
Between position, the slurry flows into the discharging opening that the other end of pipe is connected to the second heat exchanger bottom.
10. the method that the F- T synthesis system any one of a kind of utilization claim 1-9 carries out F- T synthesis, the side
Method includes：
F- T synthesis are carried out using the paste state bed reactor；The extraction paste state bed reactor is treated using the first defecator
Liquid phase discharging filtered；Gas-liquid point is carried out to the filtrate from first defecator using first segregation apparatuss
From to obtain gas-phase product and liquid product；Using second segregation apparatuss to the gas phase from the paste state bed reactor
Discharging carries out gas-liquid separation；With in the presence of vapor, using the stripper to the gas from first segregation apparatuss
Phase product and liquid product, and stripping separation is carried out from the liquid product of second segregation apparatuss, and pass through the product
Grade product is discharged in thing outlet.
11. methods according to claim 10, it is characterised in that the charging solid content of first segregation apparatuss is not more than
60ppm；The bottom of towe discharging flow of the stripper is 0.3-0.5 times of the liquid phase feeding flow of the stripper, and solid content is institute
State the first segregation apparatuss charging solid content 2-3.8 times, wherein, the flow is volume flow.
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