CN107760343A

CN107760343A - A kind of gas-solid separating method of the pyrolytic reaction product of the powder containing carbon hydrogen element

Info

Publication number: CN107760343A
Application number: CN201610723179.2A
Authority: CN
Inventors: 王庆元
Original assignee: 王庆元
Current assignee: Victory Polytron Technologies Inc
Priority date: 2016-08-21
Filing date: 2016-08-21
Publication date: 2018-03-06

Abstract

The present invention relates to a kind of gas-solid separating method of the pyrolytic reaction product of the powder containing carbon hydrogen element, it is suitable for pulverized coal pyrolysis process, pulverized coal pyrolysis reaction product by be arranged in settler by slightly revolving, the piece-rate system S10 of main rotation composition isolates most of half and defocused obtains coal gas S10V, coal gas S10V into independent piece-rate system S30 S301 are partially separated as coal gas S301UV, lose heart down the lower discharging S301DSV that S301DV and semicoke S301DS is formed, S301DSV into S30 S302 are partially separated as coal gas S302V and semicoke S302DS, S301UV, S302V enters promoting the circulation of qi respectively, liquid separates and recovery gained coal gas joint processing；The high temperature purification coal gas without tar can be injected to S10V makes its heating prevent tar fog from oozing now；S301UV, S302V separation and recovery step are usually using washing fractionating column.

Description

A kind of gas-solid separating method of the pyrolytic reaction product of the powder containing carbon hydrogen element

Technical field

The present invention relates to a kind of gas-solid separating method of the pyrolytic reaction product of the powder containing carbon hydrogen element, it is suitable for fine coal Pyrolytic process, pulverized coal pyrolysis reaction product is by being arranged in being separated by thick rotation, the main piece-rate system S10 formed that revolves in settler Go out most of half it is defocused obtain coal gas S10V, coal gas S10V into independent piece-rate system S30 S301 are partially separated as coal gas S301UV, lower discouraged S301DV and semicoke S301DS compositions lower discharging S301DSV, S301DSV into S30 S302 parts are divided Coal gas joint obtained by air-liquid separation and recovery is carried out respectively and is added from for coal gas S302V and semicoke S302DS, S301UV, S302V Work；The high temperature purification coal gas without tar can be injected to S10V makes its heating prevent tar fog from oozing now；S301UV, S302V's Step is separated and recovered usually using washing fractionating column.

Background technology

Powder of the present invention containing carbon hydrogen element, refer to produce containing oil vapour in pyrolytic process of the present invention The powder containing carbon, protium, such as the low-disintegration coal powder that volatile matter content is high.

Large coal mine such as low-disintegration coal ore deposit generally use mechanization fully mechanized mining technology is modernized to improve coal mining efficiency, reduce Cost, the fine coal yield in its coal extraction product is about 60~70%, turns into main product, therefore the deep conversion of fine coal and comprehensive The principal status of public economy that will be occupied modern low-disintegration coal charcoal using technology and utilize technology is closed, a branch field of fine coal processing is " fine coal sub-prime classified utilization ", wherein pulverized coal pyrolysis is considered as the technological approaches for having economic competitiveness.

Pulverized coal pyrolysis process of the present invention, refer to that using voluminous coal tar be process goal in suitable temperature range The pulverized coal pyrolysis process of interior operation.

The major product of pulverized coal pyrolysis process is tar, coal gas, semicoke, wherein tar be considered as potential age deduction most Big product, it is usually desirable to improve its yield and/or hydrogen content.

Pulverized coal pyrolysis product belongs to gas-solid miscible fluids, in order to obtain the products such as coal gas, tar and carry out deep processing, just The clear gas solid separation of pulverized coal pyrolysis product must be completed, in order to meet coal gas, tar secondary processing process to solid in raw material The depth separation of the restrictive requirement of content, just the semicoke dust particularly fine powder in necessary deep removal coal gas, this is relation One critical process of pulverized coal pyrolysis technique success or failure, in fact, the pulverized coal pyrolysis technique in many exploitations is exactly because this gas Gu separating step is difficult to Effec-tive Function steady in a long-term and going no further can not move towards to be commercialized.

The main target of the coal gas of pulverized coal pyrolysis product and the commercialization separation method of coke breeze is：Ensureing fortune steady in a long-term Under conditions of row, the separation accuracy for improving coal gas and semicoke dust is to improve solid in semicoke dust recovery rate, reduction coal gas to contain Measure, laid the foundation for coal gas, the following process of tar, while separation method must be easy to industrial reliable amplification to be easy to raising single Set system processing capacity obtains notable so as to reduce cost of unit engineering and specific energy consumption only in said one or several targets Break through, commercialized pulverized coal pyrolysis product gas solid separation technology could be turned into.

The coal gas of existing pulverized coal pyrolysis product and the separation method of coke breeze, main use centrifugation such as cyclonic separation, The methods of multi-medium filtering, gravitational settling, ammonia scrubbing, in terms of engineering application state, in the prevalence of operation stability difference such as Separation equipment or pipe-line system easily form tar heavy constituent deposition and block i.e. that the cycle of operation is short, low separation efficiency i.e. dedirt coal gas The problem of dust content is high.The root that above mentioned problem be present essentially consists in：

1. without suitable pyrolysis way is selected, cause the tar heavy constituent droplet containing over-saturation in coal gas；

2. without the suitable insulation heat tracing mode of selection, the cooling of gas-solid product cyclone separator is caused to separate out tar heavy constituent Droplet；

3. without suitable quick separating mode is selected, coal gas separator cooling is caused to separate out a large amount of tar heavy constituent mists Drop；

4. without multistage enough classification separate mode is selected, cause that coal gas piece-rate system dedirt precision is low, dedirt coal gas Dust content is high.

In order to solve the above problems, the present invention just 2.~5. item propose improved method, main target is to prevent or prevent out Existing tar droplet, the big-and-middle solid particle of taxonomic revision and small micro- solid particle, means are to prevent or prevent coal gas cooling, repeatedly divide Level separates large, medium and small micro- solid particle.

The built-in gas solid separation system S10 of the present invention, it is to use for reference petroleum based heavy fuel oils catalytic cracking reaction regenerative system The gas solid separation system (thick rotation, the main rotation of one-level, the main rotation of two level) being arranged in settler of riser reaction product and propose, Therefore, correlation technique can be as the reference technology or background technology of the present invention.

The external gas solid separation system S30 of the present invention, it is to use for reference petroleum based heavy fuel oils catalytic cracking reaction regenerative system Flue gas gas solid separation rear portion system (external flue gas multitube guide-vane three revolve gas-solid separator) and propose, therefore, related skill Art can be as the reference technology or background technology of the present invention.

A kind of gas-solid separating method of the pyrolytic reaction product of powder containing carbon hydrogen element of the present invention, has no report.

The inventive method can be applied to the pyrolytic reaction process of a variety of solid powders containing carbon hydrogen element, can also be applied to 2 kinds or the joint processing of a variety of separate sources powders.

Therefore, the first object of the present invention is to propose a kind of gas-solid of the pyrolytic reaction product of the powder containing carbon hydrogen element Separation method, using built-in piece-rate system S10 and external piece-rate system S30.

The second object of the present invention is to propose a kind of gas solid separation of the pyrolytic reaction product of the powder containing carbon hydrogen element Method, its heating is set to prevent that tar fog from oozing to coal gas S10V injection high-temperature gases existing.

The third object of the present invention is to propose a kind of gas solid separation of the pyrolytic reaction product of the powder containing carbon hydrogen element Method, S301 and S302 two parts are included using built-in piece-rate system S10 and external piece-rate system S30, S30.

The fourth object of the present invention is to propose a kind of gas-solid separating method of pulverized coal pyrolysis reaction product.

The fifth object of the present invention is to propose a kind of pulverized coal pyrolysis method.

The content of the invention

A kind of gas-solid separating method of the pyrolytic reaction product of the powder containing carbon hydrogen element of the present invention, it is characterised in that include Following steps：

(1) completed in one-level pyrolytic reaction process R10, the powder R10FS containing carbon hydrogen element by pyrolysis reactor R10E Pyrolytic reaction R10R is converted into one-level pyrolytic reaction gas-solid product R10P；

(2) in gas solid separation section S10, one-level pyrolytic reaction gas-solid product R10P by using cyclone separator segregative line System is separated into one section of separation coal gas S10PV and one section of separation semicoke S10PL；

The cyclone separator that gas solid separation section S10 is used, the top being arranged in the settler R20E described in step (3) are empty Between in, the hot environment of the upper space in settler R20E forms the outside for the cyclone separator that gas solid separation section S10 is used Hot environment；

Gas solid separation section S10, including at least cyclonic separation step S101, S102 of 2 grades of serial operations；

One section of separation semicoke S10PL includes the semicoke of gas solid separation section S10 discharges at different levels；

The coal gas of gas solid separation section S10 afterbody cyclone separator discharge is used as one section of separation coal gas S10PV；

In S101, one-level pyrolytic reaction gas-solid product R10P enters thick rotation S101 and is separated into thick rotation coal gas S101V and thick rotation Semicoke S101S；

In S102, it is thick revolve coal gas S101V by pipeline enter the main rotation S102 of one-level be separated into the main rotation coal gas S102V of one-level with The main rotation semicoke S102S of one-level；

One section of separation semicoke S10PL includes thick rotation semicoke S101S and the main rotation semicoke S102S of one-level；

(3) in two level pyrolytic reaction process R20, two level pyrolysis reactor R20E or settler R20E, at least one are used The reaction compartment for dividing one section of separation semicoke S10PL to enter two level pyrolytic reaction process R20, main body flow direction is to flow from top to bottom, Carry out the second pyrolytic reaction R20R；Two level pyrolysis char R20PS discharge two level pyrolytic reaction processes R20；

(4) in gas solid separation process S20, containing after two level pyrolytic reaction process R20 solid powder main body bed is left Dirt two level is pyrolyzed coal gas R20EPV, and discharge gas solid separation process S20 is separated into by using the piece-rate system S20 of cyclone separator Two level pyrolysis coal gas R20PV and return to the backflow semicoke S20PS in two level pyrolytic reaction space；

(5) in pipeline PP, one section of separation coal gas S10PV enters step (6) the gas solid separation section by pipeline PP S30；

(6) in gas solid separation section S30, cyclonic separation step S301 is set；

Enter the multitube parallel separation that more cyclone tubes are set in separating step S301, one section of separation coal gas S10PV System, using the lower discouraged mode of operation of discharge, it is separated into discharging S301DSV under coal gas S301UV and gas-solid, discharging under gas-solid S301DSV includes semicoke S301DS and lower discouraged S301DV.

Gas solid separation section S30 of the present invention can set cyclonic separation step S301, S302 of serial operation, and its feature exists In：

(6) in gas solid separation section S30, cyclonic separation step S301, S302 of serial operation is set；

Enter the multitube parallel separation that more cyclone tubes are set in separating step S301, one section of separation coal gas S10PV System, using the lower discouraged mode of operation of discharge, it is separated into discharging S301DSV under coal gas S301UV and gas-solid, discharging under gas-solid S301DSV includes semicoke S301DS and lower discouraged S301DV；

Discharging S301DSV enters the piece-rate system for setting cyclone tube under separating step S302, gas-solid, using discharge Discouraged mode of operation down, is separated into discharging S302DSV under coal gas S302UV and gas-solid, and discharging S302DSV includes half under gas-solid Burnt S302DS and lower discouraged S302DV；

In semicoke storage tank V3022, discharging S302DSV is separated into coal gas V3022V and semicoke V3022S, coal gas under gas-solid V3022V is from top let-down vessel V3022, and semicoke V3022S is from bottom let-down vessel V3022.

The present invention, in gas solid separation section S30, in separating step S301, it is more that usual one section of separation coal gas S10PV enters setting The multitube parallel piece-rate system of root guide vane formula cyclone tube.

The present invention, in gas solid separation section S30, cyclonic separation step S301, S302 of serial operation can be set；

Enter the more of more guide vane formula cyclone tubes of setting in separating step S301, one section of separation coal gas S10PV Pipe parallel connection piece-rate system；

Discharging S301DSV enters the segregative line for setting guide vane formula cyclone tube under separating step S302, gas-solid System,

The separator S302E that the separator S301E that separating step S301 is used uses with separating step S302 is set at one Upper and lower in standby housing S30E to be longitudinally arranged, S301E is located on S302E；

Discharging S302DSV enters semicoke storage tank V3022 process under gas-solid, is controlled by weighted valve or flutter valve.

The present invention, gas solid separation section S10, cyclonic separation step S101, S102, S103 of 3 grades of serial operations can be included；

The main rotation coal gas of two level is separated into the main rotation S103 of two level by pipeline in S103, one-level main rotation coal gas S102V The S103V and main rotation semicoke S103S of two level；

One section of separation semicoke S10PL includes thick rotation semicoke S101S, the main rotation semicoke S102S of one-level and the main rotation semicoke of two level S103S；

The coal gas of afterbody cyclone separator discharge is that the main rotation coal gas S103V of two level is used as one section of separation coal gas S10PV.

The present invention, gas solid separation section S10, can include cyclonic separation step S101, S102 of 4 grades of serial operations, S103, S104；

The main rotation coal gas of three-level is separated into the main rotation S104 of three-level by pipeline in S104, two level main rotation coal gas S103V The S104V and main rotation semicoke S104S of three-level；

One section of separation semicoke S10PL includes thick rotation semicoke S101S, the main rotation semicoke S102S of one-level, the main rotation semicoke of two level The S103S and main rotation semicoke S104S of three-level；

The coal gas of afterbody cyclone separator discharge is that the main rotation coal gas S104V of three-level is used as one section of separation coal gas S10PV.

The present invention, separating step S301 discharge coal gas S301UV, into separation and recovery step S700, can enter promoting the circulation of qi, Liquid separates, or enters promoting the circulation of qi, oil, water separation, and separation and recovery step S700 carries out air-liquid point usually using washing fractionating column ST700 From.

The present invention, separating step S302 discharge coal gas S302UV, into separation and recovery step S800, can enter promoting the circulation of qi, Liquid separates, or enters promoting the circulation of qi, oil, water separation, and separation and recovery step S800 carries out air-liquid point usually using washing fractionating column ST800 From.

The present invention, in one-level pyrolytic reaction process R10, the particle diameter of the powder R10FS containing carbon hydrogen element is usually 0~6 milli Rice, 0~2 millimeter is generally, one or more of the powder R10FS in following materials containing carbon hydrogen element：

1. low rotten fine coal；

2. high rotten fine coal；

3. oil shale powder；

4. other can produce the solid powder containing oil vapour in pyrolytic process.

The present invention, one-level pyrolytic reaction process R10 operating pressure are usually：0.1~6.0MPa, with absolute manometer.

The present invention, in one-level pyrolytic reaction process R10, the powder R10FS containing carbon hydrogen element is usually fine coal；

One-level pyrolytic reaction process R10 reacting product outlet temperature is one-level pyrolytic reaction process cessation reaction temperature： Generally generally 350~700 DEG C, generally 400~600 DEG C, preferably 420~500 DEG C.

The present invention, in pipeline PP, after one section of separation coal gas S10PV and high temperature concurrent heating gas VT100 is mixed into gaseous mixture XV Operation temperature into step (6) gas solid separation the section S30, XV is higher than the logistics XV dew-point temperatures of itself；Generally, coal gas 50~300 DEG C of S13V temperature；Generally, high temperature concurrent heating gas VT100 standard state volume flow is one section of separation coal gas S10PV standard The 5~25% of state volume flow, higher than one section separation coal gas S10PV operation temperature at least 5~20 of gaseous mixture XV operation temperatures ℃；The volumetric concentration of carbon four and its above hydrocarbon component is desirably no more than 0.05% in high temperature concurrent heating gas VT100；At least a portion is high Temperature compensation hot gas VT100, coal gas after coal gas S301UV deoiling treatment is can come from, form circulation logistics.

The present invention, the gentle solid separation process S20 of two level pyrolytic reaction process R20 common mode of operation are：

(3) two level pyrolytic reaction is entered in two level pyrolytic reaction process R20, one section of separation semicoke S10PL of at least a portion Process R20 reaction compartment, main body flow direction is to flow from top to bottom, and generation is contacted with the gas stripping gas V22V flowed from bottom to top and is risen Temperature effect carries out the second pyrolytic reaction R20R；Two level pyrolysis char R20PS discharge two level pyrolytic reaction processes R20；

Two level pyrolytic reaction process R20 Gas-particle Flows state, is usually expressed as dispersion fluidized bed；

(4) in gas solid separation process S20, the pyrolysis coal gas R20EPV of the dust-laden two level after solid powder main body bed is left, Gas solid separation, gained dedirt two level are completed by the gas solid separation system S20 for the cyclone separator at least using 2 grades of serial operations Coal gas R20PV discharge gas solid separation processes S20, S20 and S10 is pyrolyzed at least partly to share.

The present invention, fluidisation can be set to burn course of reaction R50, it is characterised in that：

(7) course of reaction R50 is burnt in fluidisation, the semicoke based on two level pyrolysis char R20PS burns reaction into fluidisation Space, contacted with the oxygen-containing gas flowed from bottom to top, fluid bed occurs and burns reaction R50R, produces high-temperature oxydation semicoke R50PS and flue gas YQ, flue gas YQ burn course of reaction R50 from upper space discharge fluidisation；High-temperature oxydation semicoke R50PS discharge streams Course of reaction R50 is burnt in change；Generally, ash-laden gas R50E-YQ in the device for the top dilute phase section that fluidisation burns reaction compartment, passes through Be arranged in fluidisation burn reactor R50E internal upper parts space cyclone separation system S5 dedirts be separated into flue gas YQ and backflow semicoke Dust R50E-RS；Generally, flue gas YQ, which leaves cyclone separation system S5 and discharges fluidisation, burns reactor R50E；Generally, whirlwind point The semicoke dust R50E-RS of cyclone dip-leg discharge from system S5 returns to fluidisation and burns reaction compartment cyclic process；It is logical Often, at least a portion high-temperature oxydation semicoke R50PS uses as the first solid thermal carriers R10KS.

The present invention, course of reaction R50 can be burnt in fluidisation, external warmer R50-OUT-HX is set, discharge fluidisation is burnt After course of reaction R50 thermal oxide semicoke enters external warmer R50-OUT-HX and takes thermal medium indirect heat exchange to reduce temperature, row Go out external warmer R30-OUT-HX.

The present invention, course of reaction R50 can be burnt in fluidisation, external warmer R50-OUT-HX is set, carrys out self-fluidized type and burns Course of reaction R50 thermal oxide semicoke enters external warmer R50-OUT-HX and takes thermal medium indirect heat exchange to reduce temperature, discharge External warmer R50-OUT-HX cooling oxidation semicoke returns to fluidisation and burns course of reaction R50 recyclings.

The present invention, in pipeline PP, after one section of separation coal gas S10PV and high temperature concurrent heating gas VT100 is mixed into gaseous mixture XV Operation temperature into step (6) gas solid separation the section S30, XV is higher than the logistics XV dew-point temperatures of itself；At least partially High temperature concurrent heating gas VT100 is the gas after fluidisation burns course of reaction R50 indirectly heats, and high temperature concurrent heating gas VT100 media can Think coal gas after purifying.

The present invention, can be that fluidisation is burnt in reactor R50E devices in two level pyrolytic reaction process R20, gas stripping gas V22V The indirect heat exchanger R50-HX discharges of dilute phase space arrangement take hot gas, can be the outsides half that fluidisation burns reactor R50E Burnt heat exchanger discharge takes hot gas.

The present invention, gas solid separation section S30 technology controlling and process target are：

In semicoke storage tank V3022, discharging S302DSV is separated into coal gas V3022V and semicoke V3022S, coal gas under gas-solid V3022V is from top let-down vessel V3022, and semicoke V3022S is from bottom let-down vessel V3022；

Discouraged S301DV standard state volume flow RK down, one section of standard state for separating coal gas S10PV is fed with S30 The ratio between volume flow R0 is defined as K, i.e. K=RK/R0, and K values are usually 0.2%~10%, generally 1.0%~5.0%.

The present invention, the overall operation target of each step are usually：

(1) in one-level pyrolytic reaction process R10, the powder R10FS containing carbon hydrogen element is fine coal, and pulverized coal particle size is 0~6 milli Rice；

One-level pyrolytic reaction process R10, using riser fluidized bed pyrolysis reactor, the first solid thermal carriers R10KS is Carry out the high-temperature oxydation semicoke that self-fluidized type burns course of reaction R50；

One-level pyrolytic reaction process R10 reaction time is 0.1~10s, and riser reacting product outlet temperature is one-level Pyrolytic reaction process cessation reaction temperature is 400~500 DEG C；

First solid thermal carriers R10KS weight is 1~30 with fine coal R10FS weight ratios；

(2) solids content is less than 50 grams/cubic metre in gas solid separation process S10, one section of separation coal gas S10PV；

(3) in two level pyrolytic reaction process R20 reaction compartment, 2~12 secondary herringbone baffle plates or ring baffle, two level are set The temperature of the main pyrolysis section of pyrolytic reaction process is 460~700 DEG C；

Two level pyrolysis section bottom is passed through 450~650 DEG C of gas stripping gas V22V and carries out tar steam stripping, and gas stripping gas V22V passes through Flow up after the semicoke bed of material and be pyrolyzed into two level pyrolytic reaction process R20 two level in coal gas product；

(4) in gas solid separation process S20, thick rotation and main rotation of the two level pyrolysis coal gas product by gas solid separation process S10 Between all gaps open two level pyrolytic reaction space into main whiz, be mixed into promoting the circulation of qi in main medial rotation and one-level pyrolysis coal gas divides admittedly From；

(5) in pipeline PP, one section of separation coal gas S10PV enters after being mixed into gaseous mixture XV with high temperature concurrent heating gas VT100 Step (6) gas solid separation the section S30, XV operation temperature are higher than the logistics XV dew-point temperatures of itself.

(6) solids content is less than 2 grams/cubic metre in gas solid separation section S30, coal gas S301UV.

The present invention, the overall operation target of each step are generally：

(1) it is low rotten fine coal in one-level pyrolytic reaction process R10, the powder R10FS containing carbon hydrogen element, pulverized coal particle size is 0~6 millimeter；

One-level pyrolytic reaction process R10 reaction time is 1.0~6s, and riser reacting product outlet temperature is one-level heat It is 430~470 DEG C to solve course of reaction cessation reaction temperature；

First solid thermal carriers R10KS weight is 3~15 with fine coal R10FS weight ratios；

(2) solids content is less than 10 grams/cubic metre in gas solid separation process S1, one section of separation coal gas S10PV；

(3) in two level pyrolytic reaction process R20 reaction compartment, 2~12 secondary herringbone baffle plates or ring baffle, two level are set The temperature of the main pyrolysis section of pyrolytic reaction process is 480~600 DEG C；

(4) in gas solid separation process S20, two level pyrolysis coal gas product is by gas solid separation process S10 slightly rotation and main rotations Between all gaps enter top whiz and open two level pyrolytic reaction space, on top, medial rotation and one-level pyrolysis coal gas are mixed into row gas solid separation；

(5) in pipeline PP, one section of separation coal gas S10PV enters after being mixed into gaseous mixture XV with high temperature concurrent heating gas VT100 Step (6) gas solid separation the section S30, XV operation temperature are higher than the dew-point temperature of any component.

(6) solids content is less than 1 gram/cubic metre in gas solid separation section S30, coal gas S301UV.

The present invention, the overall operation target of each step are preferably：

(1) in one-level pyrolytic reaction process R10, the R10FS of powder containing carbon hydrogen element is the low rotten fine coal of high volatile, powder Coal particle size is 0~2 millimeter；

One-level pyrolytic reaction process R10 reaction time is 2.5~4s, and riser reacting product outlet temperature is one-level heat It is 440~460 DEG C to solve course of reaction cessation reaction temperature；

First solid thermal carriers R10KS weight is 6~10 with fine coal R10FS weight ratios；

(2) solids content is less than 4 grams/cubic metre in gas solid separation process S1, one section of separation coal gas S10PV；

(3) in two level pyrolytic reaction process R20 reaction compartment, 2~12 secondary herringbone baffle plates or ring baffle, two level are set The temperature of the main pyrolysis section of pyrolytic reaction process is 480~530 DEG C；

(6) solids content is less than 0.5 gram/cubic metre in gas solid separation section S30, coal gas S301UV.

The present invention, the riser fluidized bed pyrolysis reactor R10E that one-level pyrolytic reaction process R10 is used, it is pyrolyzed with two level The two level fluidized bed pyrolysis reactor R20E that course of reaction R20 is used, can form unit equipment.

The present invention, the two level fluidized bed pyrolysis reactor R20E that two level pyrolytic reaction process R20 is used, burns instead with fluidisation The fluid bed that the process R50 of answering is used burns reactor R50E, can form unit equipment.

The present invention, riser fluidized bed pyrolysis reactor R10E that one-level pyrolytic reaction process R10 is used, two level pyrolysis are anti- Two level fluidized bed pyrolysis reactor R20E that the process R20 of answering is used, fluidisation are burnt the fluid bed that course of reaction R50 is used and burnt instead Device R50E is answered, unit equipment can be formed.

The present invention, the two level fluidized bed pyrolysis reactor R20E that two level pyrolytic reaction process R20 is used, fluidisation burn reaction It is vertical equipment that the fluid bed that process R50 is used, which burns reactor R50E, and from locus, absolute altitude is said, its mutual alignment relation Can be：The bottom that fluid bed burns reactor R50E is lower than settler R20E bottom, and settler R20E is discharged final Pyrolysis char burns reactor R50E bottom by material position difference inflow fluid bed.

The present invention, the two level fluidized bed pyrolysis reactor R20E that two level pyrolytic reaction process R20 is used burn instead with fluidisation The fluid bed that the process R50 of answering is used burns reactor R50E, can form coaxial-type unit equipment；

It is coaxial-type Vertical Combination equipment that coaxial-type, which refers to that settler R20E, fluid bed burn reactor R50E, from sky Between position relationship say that its mutual alignment relation is：Fluid bed surrounds settler with burning reactor R50E space segment R20E space；The pyrolysis char of bottom space from settler R20E flows into fluid bed by standpipe and plug valve and burns reaction Device R50E lower space.

The present invention, each step operation pressure are：

(1) one-level pyrolytic reaction process R10 operating pressure is：0.1~6.0MPa, with absolute manometer；

(2) two level pyrolytic reaction process R20 operating pressure is：0.1~6.0MPa, with absolute manometer；

(7) operating pressure that fluidisation burns course of reaction R50 is：0.1~6.0MPa, with absolute manometer.

Brief description of the drawings

Fig. 1 is that a kind of flow of the embodiment for the gas solid separation process that the present invention is applied to pulverized coal pyrolysis reaction product is shown It is intended to.

Fig. 1 is height block form pulverized coal pyrolysis system；Height block form refers to that settler R20E, fluid bed burn instead It is vertical equipment to answer device R50E, and from locus, absolute altitude is said, its mutual alignment relation is：Fluid bed burns reactor R50E's Bottom is lower than settler R20E bottom, and the final pyrolysis char of settler R20E discharges can flow automatically by material position difference into becoming a mandarin Change the bottom that bed burns reactor R50E.Do not have to represent the flow that fluid bed burns reactor R50E systems in figure.Settler R20E, because with certain pyrolysis function, alternatively referred to as two level pyrolysis reactor.

As shown in figure 1, R10E is lifting tubular type one-level pyrolysis reactor, lifting gas R10FV enters through pipeline P101 to be arranged Flowed up after the distributor R10FV-SB distribution of R10E bottoms, fine coal FM (i.e. R10FS) is through pipeline P102, the first solid thermal Carrier semicoke R10KS through pipeline P103 enter R10E bottoms mixed zone R10E-1 lifting gas R10FV effect under form fluid bed Moved up along riser, the first pyrolytic reaction of fine coal R10R during which occurs；The material of the first pyrolytic reaction is completed as One pyrolytic reaction effluent R10P discharges R10E from open top R10E-OUT, and R10P is by the coal air and heat comprising tar component Solve the gas-solid mixed phase logistics of semicoke composition.

As shown in figure 1, S10 is the first pyrolytic reaction effluent R10P gas solid separation system, settler R20E is arranged in The tip position of inner space.

Fig. 2 is the thtee-stage shiplock separation process detail drawing of the gas solid separation system S10 in Fig. 1, and the thick S101 that revolves separates for one-level, The main rotation S102 of one-level is the second-order separation, and the main rotation S103 of two level separates for three-level.

The connected mode signal that Fig. 3 is the thick rotation S101 and the main rotation S102 of one-level of the gas solid separation system S10 in Fig. 2 is detailed Figure.As shown in figure 3, slightly all gaps be present between rotation S101 exit gas conveyance conduit and the gas feed mouth of main rotation, as reception The charging aperture of settler R20E dust-laden coal gas.

As shown in Fig. 2 one-level pyrolytic reaction effluent R10P enters thick rotation S101 through pipe P105, the thick S101 that revolves completes one-level Gas solid separation, it is thick revolve powder lower into settler R20E inner spaces along dipleg P106 and typically flow into dense bed region to prevent Only dust is excessively flown upward；Thick rotation coal gas containing dust sprays into the feed pipe P108 for the main rotation S102 of one-level being flexible coupling along pipe P107, The main rotation S102 of one-level completes two level gas solid separation, and the main rotation powder of one-level lowers into settler R20E inner spaces along dipleg P109 And typically flow into dilute-phase leanphase fluidized bed region；The main rotation coal gas of one-level containing a small amount of dust enters the main rotation of two level being directly connected to along pipe P111 S103, the main rotation S103 of two level complete three-level gas solid separation, and the main rotation powder of two level is lowered into settler R20E along dipleg P112 Portion space simultaneously typically flows into dilute-phase leanphase fluidized bed region, and the main coal gas that revolves of dedirt two level is along pipe P115 discharge systems S10E.

As shown in figure 3, in system S10, the thick rotation coal gas containing dust sprays into the main rotation of one-level being flexible coupling along pipe P107 S102 feed pipe P108, Fig. 3 illustrate one kind and are flexible coupling mode, and feed pipe P108 head is that an expanding horn mouth opens Mouthful P1081, pipe P107 head P1071 are one and extend into horn mouth P1081 sky with footpath extension opening P1071, P1071 In, all gaps be present between thick screw outlet gas transmission pipeline and the gas feed mouth of pipe of main rotation.

As shown in figure 1, R20E is two level pyrolysis reactor, R20E inner space, comprises at least and set according to process function Put the headroom V21 of cyclone separation system, one section of sedimentation degassing space or two level pyrolytic reaction space for separating semicoke S10PL V22。

It is generally desirable to two level pyrolytic reaction space present particulate fluidization bed form, now, top be dilute phase space V21, under Portion is close phase space V22, and close phase space V22 bottoms generally have stripping gas V22 to flow up.

As shown in figure 1, the coke breeze in system S10 dipleg enters two level pyrolytic reaction process R20, i.e. whirlwind by gravity Coke breeze in separator dipleg enters two level pyrolytic reaction process R20 space by gravity.

As shown in figure 1, one section into settler R20E reaction compartments separates semicoke S10PL, it is certainly to produce main body flow direction Simultaneously flow direction is varied multiple times by baffle plate in upper and lower flowing, and the structure type of baffle plate has a variety of such as setting polylith herringbone baffle plates, more Block annular slab etc., one section separates the second pyrolytic reaction R20R of semicoke S10PL progress in above process；Complete two level pyrolytic reaction Material be divided into descending two level pyrolysis char R20EPS and two level pyrolysis dust-laden coal gas R20EPV, two level pyrolysis char after degassing R20PS discharges from the bottom of settler R20E reaction compartments through pipeline P2205, valve, pipeline P2206, two level pyrolysis char R20PS may finally go fluid bed to be stored after burning reactor R50E or cooling.

As shown in figure 1, two level is pyrolyzed dust-laden coal gas R20EPV, its gas solid separation process S20 flows out with one-level pyrolytic reaction The gas solid separation section S10 of thing, main rotation system can be partly or entirely shared, receive two level pyrolysis dust-laden coal gas R20EPV charging aperture For " all gaps between thick screw outlet gas transmission pipeline and the gas feed mouth of main rotation ", two level be pyrolyzed dust-laden coal gas R20EPV from Open two level pyrolytic reaction space and enter main precession row gas solid separation.

As shown in figure 1,450~650 DEG C of gas stripping gas V22V enter in V22 the distributor V22V-SB arranged along pipeline P2201 Enter the bottom of two level pyrolytic reaction SPACE V 22 after distribution, stripping vapor by air lift after the semicoke bed of material and carry tar steam to In the upper two level pyrolysis coal gas product for flowing and eventually entering into two level pyrolytic reaction process R20.

Reactor R50E is burnt in fluid bed, such as two level pyrolysis char of the final pyrolysis char from settler R20E R20PS, enters R50E bottoms mixing chamber R50E-1 after piping, guiding valve, pipeline, and oxygenous lifting gas R50-ZF enters arrangement Flowed up after the distributor V5-SB distributions of R50E bottoms, form semicoke fluidized bed combustion, the flue gas of generation of burning is along stream Change bed burns reactor R50E and moves up and carry semicoke dust secretly.Fluid bed burns in reactor R50E device and burns flue gas R50EPV, its gas solid separation process S50 are arranged in the tip position that fluid bed burns reactor R50E inner spaces, by 1 grade of rotation Wind separator or 2 grades of serial operation or multi-cyclone composition；Gas solid separation process S50, gained is de- after separating coke breeze Cloud of dust gas YQ discharge fluid beds burn reactor R50E and go pressure energy recovery and/or heat recovery and/or dust depth piece-rate system Flue gas YQ is discharged into air after processing, generally processing or part recycles；Gas solid separation process S50, the powder in separator dipleg Jiao burns reaction compartment cyclic process by what gravity returned to that fluid bed burns reactor R50E.

As shown in figure 1, the hot semicoke conveyed by pipeline, guiding valve and pipeline P103, as the first solid thermal carriers R10KS Into one-level pyrolysis reactor R10E.

As shown in figure 1, one section of separation coal gas S10PV enters later separation recovery system S30 by pipeline P115.

It distributor R10FV-SB or V22V-SB, can be any appropriate form in Fig. 1, for example can be provided with for one multiple The shower nozzle of the top cover of aperture is an annular spread pipe for being provided with multiple apertures or be a top cover for being provided with multiple apertures Nozzle chamber.

Fig. 4 is the separator S30E of the external gas solid separation system S30 in Fig. 1 detail of construction, gas solid separation system The regenerated flue gas gas solid separation rear portion system that S30E structure is similar to petroleum based heavy fuel oils catalytic cracking reaction regenerative system is i.e. outer Put formula flue gas three-stage cyclone separator -- the gas-solid separator of multiple guide-vane cyclone tube parallel operations.

As Figure 1 and Figure 4, S30E central tube P3011 is entered along pipeline P118, through multiple gas outlet K3011 (in figure Show 2) enter unstripped gas sub-air chamber V3011；Sub-air chamber V3011 is with dividing plate PL3011, dividing plate PL3012, housing VE3011 And guide-vane cyclone tube XF3011 shells are the space that border is formed, guide-vane cyclone tube XF3011 can set 1 It is individual or 2 or multiple；In sub-air chamber V3011, gas enters the cyclone tube for setting guide vane through air inlet a XF3011, dedirt gas S301UV enter dust-removing gas collection chamber V3012 through air guide mouth of pipe b, come together in collection chamber V3012 dedirt Gas S301UV drain separators S30E enters separation and recovery system S700 through pipeline P3051.

As Figure 1 and Figure 4, in sub-air chamber V3011, gas enters the cyclonic separation for setting guide vane through air inlet a Pipe XF3011, the semicoke dust S301DS of abjection and lower discouraged S301DV are through opening c inflow spaces V3013；Semicoke dust The gas-solid mixing material S301DSV of S301DS and lower discouraged S301DV compositions goes S30E hypomere S302E to carry out Pyatyi separation.

As Figure 1 and Figure 4, Pyatyi separation is carried out in S30E hypomere S302E, using 1 or 2 or multiple settings are led The cyclone tube XF3021 (1 is shown in figure) of blade is flowed, gas-solid mixing material S301DSV is led through air guide mouth of pipe p into setting The cyclone tube XF3021 of blade is flowed, dedirt gas S302UV leaves S302E into pipeline P3081 through air guide mouth of pipe q and entered Separation and recovery system S800.

As Figure 1 and Figure 4, Pyatyi separation is carried out in S30E hypomere S302E, uses the whirlwind point that guide vane is set From pipe XF3021, gas-solid mixing material S301DSV enters the cyclone tube XF3021 for setting guide vane through air guide mouth of pipe p, partly The gas-solid mixing material S302DSV of coke powder dirt S302DS and lower discouraged S302DV compositions enters S302E hypomere space through opening r V3021, and into semicoke storage tank VE3022 SPACE V 3022 after valve F3021.Valve F3021 form can be the wing Valve or weighted valve.

As Figure 1 and Figure 4, the semicoke stored in semicoke storage tank VE3022 SPACE V 3022 is through piping P3095, valve Discharged after door, pipeline P3096.

As Figure 1 and Figure 4, the coal gas S302DV of discharge flows through pipeline in semicoke storage tank VE3022 SPACE V 3022 The gas S302UV of P3091 and pipeline P3081 discharges converges enters separation and recovery system S800 Combined Treatments for S302V.

The dedirt gas S301UV of collection chamber V3012 discharges, the separation that coal gas is carried out into separation and recovery process S700 are returned Receive, can carry out liquid, qi leel from, such as carry out oil, qi leel from, such as carry out oil, gas and water separation；Liquid, gas, dirt separation can be carried out, For example carry out oil, gas, dirt separation, such as progress or Oil, Water, Gas, dirt separation；Separation and recovery process S700, fluid can be used Fractionating column is washed, carries out oil wash and fractionation；Separation and recovery process S700, washing knockout tower can be used, is washed and is separated, Water containing ammonia circulation wash cooling coal gas can be used.

The dedirt gas S302V of cyclone separator XF3021 and semicoke storage tank VE3022 discharges, into separation and recovery process S800 carries out the separation and recovery of coal gas, can carry out liquid, qi leel from for example carrying out oil, qi leel from for example carrying out oil, gas and water point From；Liquid, gas, dirt separation can be carried out, for example carries out oil, gas, dirt separation, such as progress or Oil, Water, Gas, dirt separation；Separation and recovery Process S800, fluid washing fractionating column can be used, carries out oil wash and fractionation；Separation and recovery process S800, washing can be used Knockout tower, washed and separated, water containing ammonia circulation wash cooling coal gas can be used.

Separation and recovery process S700 and separation and recovery process S800, generally each works independently.

Separation and recovery process S700 and separation and recovery process S800, can partly or entirely work together, be suitable for scale Less device, can simple flow.

As shown in figure 1, separation and recovery process S700 isolates gas S700PV and other products S700P1, other products S700P1 can include water logistics, oily logistics, dust-laden logistics.Gas S700PV is through piping P701, valve F701, pipeline P702 After remove coal gas after-treatment system S900.Coal gas due to flowing through pipeline P701 occupies coal gas product overwhelming majority quantity, is main Coal gas product, therefore valve F701 is typically used as coal gas pyrolytic reaction process R10 reaction pressure control valve.

As shown in figure 1, separation and recovery process S800 isolates gas S800PV and other products S800P1, other products S800P1 can include water logistics, oily logistics, dust-laden logistics.Gas S800PV is through piping P801, flow control element F801, pipeline Coal gas after-treatment system S900 is removed after being mixed after P802 with coal gas S700PV.Because the gas volume for flowing through pipeline P801 determines S30E epimere S301E discharge lower discouraged S301DV gas flow, generally set control flow element F801 such as valves or The lower discouraged S301DV of restriction orifice or Venturi tube or critical spray nozzle, regulation or control gas flow, regulation or control S301E's Separating effect.

Embodiment

1. low rotten fine coal；

2. high rotten fine coal；

3. oil shale powder；

The present invention, the overall operation target of each step are usually：

The present invention, each step operation pressure are：

Each step specific features are described below in conjunction with overall procedure.

Fine coal FM into one-level pyrolytic reaction process R10 is R10FS, is dehydrated fine coal after usually drying, its moisture weight Amount usually less than 10%, generally below 7%, preferably are less than 5%.

Fine coal FM into one-level pyrolytic reaction process R10 is R10FS, and its granularity is usually 0.00001~6 millimeter, one As for 0.0001~3.5 millimeter, preferably be 0.001~2 millimeter.

Can be any one temperature, pressure, component composition into one-level pyrolytic reaction process R10 gas stripping gas R10FV Etc. suitable gas, the usually coal gas or producing synthesis gas from coal after vapor or nitrogen or not oxygenous flue gas or purification de-oiling Or semicoke preparing synthetic gas.

Into one-level pyrolytic reaction process R10 the first solid thermal carriers R10KS, usually reaction is burnt from fluid bed Process R50 high-temperature oxydation semicoke, the ratio of its weight flow and fine coal R10FS weight flows, determine as needed, be usually 0.5~30, it is 5~10 to be generally 3~15, preferably.

One-level pyrolytic reaction process R10, the one-level pyrolysis reactor R10E used Type of equipment determine as needed, lead to Often using lifting tubular type one-level pyrolysis reactor.

Gas solid separation section S10, usually using centrifugation formula gas-solid separation equipment element, 1 grade or 2 grades or more can be formed The gas solid separation system of level serial operation.

In one section of separation coal gas S10PV solids content be usually less than 50 grams/cubic metre, generally below 10 grams/cubic metre, compared with Good person is less than 4 grams/cubic metre.

Two level pyrolytic reaction process R20, its Type of equipment determine as needed, usually using vertical downflow system settler R20E。

The gas stripping gas of two level pyrolysis reactor bottom, generally select inert gas such as steam or nitrogen or the flue of no oxygen Gas or purification coal gas circulating air or other inert gases.

On settler R20E structures, its process function is to form fluid bed, preferably form dispersion fluidized bed and expand Bed, settler R20E inner space is broadly divided into three sections：Epimere is the de- solid space of the gas of low gas velocity, stage casing is that gas velocity is suitable Two level pyrolysis main reaction space, hypomere be stripping section.

Epimere takes off solid space for the gas of low gas velocity, therefore, it is necessary to reduces the coal gas for being pyrolyzed main reaction space from below Cross sectional flow rate, that is to say, that it is required that reducing gas flow rate needs enlarged cross section area, therefore, usual epimere is that gas is de- solid The radial section product in space is more than the radial section product that stage casing is two level pyrolysis main reaction space.

Stage casing is that the suitable two level of gas velocity is pyrolyzed main reaction space, here, two level pyrolytic reaction occurs for one-level pyrolysis char Discharge coal gas, tar steam；During one-level pyrolysis char is pyrolyzed main reaction space through two level from top to down, with The rise of temperature, one-level pyrolysis char progressively discharge coal gas, tar steam, and two level is pyrolyzed the half of the bottom discharge in main reaction space Burnt release coal gas, the ability of tar steam very little.

In stripping section, the gas stripping gas flowed up of two level pyrolysis reactor bottom stripping section is entered from bottom, generally Being uniformly distributed for initial stage is realized by gas distributor, because the effect of the gas is to carry two level pyrolysis reaction section bottom semicoke In the tar gas that includes, therefore, the flow of gas stripping gas is typically less, and gas stripping gas category is said from follow-up coal gas processing and utilization angle It should be reduced as far as possible in invalid component (vapor, nitrogen, flue gas) or circulating gas, its quantity, the section face of such stripping section Product is generally smaller.In fact, the area of section of stripping section is typically smaller than the area of section in two level pyrolysis main reaction space.

Solids content is usually less than 50 in discharge gas solid separation system S20 dedirt two level pyrolysis coal gas S20V or R20PV Gram/cubic metre, generally below 10 grams/cubic metre, preferably are less than 4 grams/cubic metre.

Gas heat carrier V22V, can be the suitable gases such as any one temperature, pressure, component composition, usually water Coal gas or producing synthesis gas from coal or semicoke preparing synthetic gas after steam or nitrogen or not oxygenous flue gas or purification de-oiling.

Fluid bed burns course of reaction R50, and the Type of equipment that fluid bed burns reactor R50E determines as needed, generally Reactor R50E is burnt using vertical fluidized bed.

As needed, fluid bed burns course of reaction R50, can discharge thermal oxide semicoke R50PS products or not discharge heat Aoxidize semicoke R50PS products；The thermal oxide semicoke R50PS of discharge is stored after recovery heat energy being cooled down by indirect heat exchanger.

As needed, fluid bed burns course of reaction R50, can set cyclic oxidation semicoke logistics R50RS heat collectors, follow Epoxidation semicoke logistics R50RS burns reaction by returning to fluid bed after defeated heat energy cooling outside indirect heat exchanger such as steam generator Process R50, now, cyclic oxidation semicoke logistics R50RS serve as the heat carrier of outer defeated heat energy.

Solids content in final dedirt coal gas S301UV, usually less than 2 grams/cubic metre, generally below 0.8 gram/cubic metre, Preferably is less than 0.2 gram/cubic metre.

Solids content in final dedirt coal gas S302V, usually less than 2 grams/cubic metre, generally below 0.8 gram/cubic metre, Preferably is less than 0.2 gram/cubic metre.

Down lose heart S302DV standard state volume flow RK, with S30E charging coal gas standard state volume flow R0 it Than being defined as K, i.e. K=RK/R0, K values are usually 0.2%~10%, are generally 0.5%~8%, are easily 1.0%~5.0%.

The advantage of the invention is that：

1. realizing tracing thermal-insulating to built-in rotation subset using the heating gas in settler R20E, high temperature circulation concurrent heating is utilized Gas ensures that the operation temperature of external rotation point charging coal gas is higher than dew point, effectively prevents the condensation of higher boiling tar component in coal gas from making Into pipeline, separation equipment blocks, it is ensured that rotation divides separative efficiency and the cycle of operation of piece-rate system；

2. using thick rotation, main rotation, three rotations method ON-LINE SEPARATION coal gas in coke breeze, improve coal gas dedirt precision, can be with In control coal gas solids content be usually less than 2 grams/cubic metre, generally below 0.6 gram/cubic metre, preferably less than 0.2 gram/it is vertical Square rice, weight dust content in the tar that coal gas isolates can be controlled to be less than 2%, coke breeze average grain diameter is usually less than 20 in tar μm, generally below 10 μm, preferably be less than 6 μm, can effectively reduce the severity of tar following process；

3. due to improving coal gas dedirt rate, therefore the raw material pulverized coal particle size of pulverized coal pyrolysis reactor can be reduced, can be with The coal charge of easy efflorescence is processed, pyrolysis rate can be improved, improves unit volume processing capacity；

4. due to improving coal gas dedirt rate, therefore the raw material pulverized coal particle size of pulverized coal pyrolysis reactor can be reduced, can be with Pyrolysis rate is improved, shortens pyrolysis time, reduces secondary pyrolysis reacting dose, beneficial to pyrolytic tar yield is improved, beneficial to raising heat Solve tar hydrogen content.

Reference examples

Factory, Shenmu, Shanxi caragana microphylla tower coal analysis data are shown in Table 1, as it can be seen from table 1 the coal belongs to special low grey, special low The jet coal of sulphur, high-volatile, category can the high-quality coals that utilize of sub-prime.

Using CN105602593A, CN105694933A method, powder after single-stage pyrolysis of coal course of reaction dry processing is set Coal, fine coal particle size range is 0~2.0 millimeter, using one-level riser pyrolytic reaction process R10, one-level pyrolytic reaction product R10P enters the three-level whirlwind point being made up of thick rotation, the main rotation of one-level, the main rotation of two level for being arranged in settler R20E headspaces Gas solid separation system S10 from device serial operation is separated into one section of separation semicoke S10PL and one section of separation coal gas S10PV, one section Separate semicoke S10PL and enter downflow system settler R20E and stripping vapor counter current contacting completion decoking oil gas task, settler The dust-laden coal gas of dilute phase section discharge imports the entrance of gas solid separation system S10 secondary cyclone at the top of R20E.One section point It is less than 3 grams/cubic metre from solids content in coal gas S10PV, usually 1.5~2.0 gram/cubic metre.

The coal gas of gas solid separation system S10 discharges, through supercooling, separation, carry out the separation and recovery of dirt, gas, oil, water. 20 DEG C of density of the tar of recovery are ton/cubic metre of density 1.131~1.150, and tar yield is (to fine coal R10FS weight ratio Example) it is 0.131~0.152.

The degassing two level pyrolysis char of settler discharge enters fluidized bed and burns reactor R50E, and combustion reaction produces temperature About 700 DEG C of heat of oxidation semicoke, the hot semicoke of partial oxidation are consolidated as one-level riser pyrolytic reaction process R10 is used first Body heat carrier, the hot semicoke of partial oxidation return to fluid bed after circulating through steam generator as the heat carrier of external warmer Reactor R50E is burnt, remaining heat of oxidation semicoke discharge fluid bed stores after burning reactor R50E recovery heat energy.

Table 2 is reference examples operating condition.

The Factory, Shenmu, Shanxi caragana microphylla tower coal analysis data of table 1

The reference examples operating condition of table 2

Sequence number	Project	Data
			1	One-level pyrolytic reaction process R10E
1.1	One-level pyrolytic reaction process R10 base pressures, MPa absolute pressures	0.180~0.186
			1.2	One-level pyrolytic reaction process R10 top pressures, MPa absolute pressures	0.170~0.176
1.3	One-level pyrolytic reaction process R10 head temperatures, DEG C	465~475
			1.4	Fine coal R10FS particle size ranges, millimeter	0~2.0
1.5	Fine coal R10FS temperature, DEG C	120~130
			1.6	First solid thermal carriers R10KS temperature, DEG C	690~710
1.7	First solid thermal carriers R10KS weight and fine coal R10FS weight ratios	7.2~8.8
			1.8	Reaction time, second	2.5~3.0
2	Pyrolytic reaction result
			2.1	Tar yield, with fine coal R10FS part by weight	0.131~0.152
2.2	Gas yield, standard cubic meter/ton coal	72~85
			2.3	Semi-coke yield, with fine coal R10FS part by weight	0.651~0.752
2.4	20 DEG C of density of tar, ton/cubic meter	1.131~1.150
			3	Fluid bed burns reactor R50E
3.1	Base pressure, MPa absolute pressures	0.200~0.210
			3.2	Top pressure, MPa absolute pressures	0.197~0.207
3.3	Heat carrier semicoke temperature, DEG C	690~710

Embodiment

Embodiment one

Based on reference examples, using gas-solid separating method of the present invention, one section of separation coal gas S10PV external gas-solid point is set From system S30, S30 includes S301 and S302 two parts, i.e. the level Four separation process comprising one-level thermal decomposition product and Pyatyi separation Process.

Level Four separation process uses more guide-vane cyclone tube XF3011 being operated in parallel.

Pyatyi separation process uses more guide-vane cyclone tube XF3021 being operated in parallel.

Solids content is less than 1.0 grams/cubic metre in final dedirt coal gas S301UV, usually 0.20~0.45 gram/cube Rice.

Solids content is less than 1.0 grams/cubic metre in final dedirt coal gas S302V, usually 0.20~0.45 gram/cube Rice.

The standard state volume flow RK of gas S302V based on lower discouraged S301DV, the standard shape with S30 charging coal gas The ratio between state volume flow R0 is defined as K, i.e. K=RK/R0, and K values are 3.5%~5.0%.

Claims

1. a kind of gas-solid separating method of the pyrolytic reaction product of the powder containing carbon hydrogen element, it is characterised in that include following step Suddenly：

(1) complete to be pyrolyzed by pyrolysis reactor R10E in one-level pyrolytic reaction process R10, the powder R10FS containing carbon hydrogen element Reaction R10R is converted into one-level pyrolytic reaction gas-solid product R10P；

(2) divided in gas solid separation section S10, one-level pyrolytic reaction gas-solid product R10P by using the piece-rate system of cyclone separator Coal gas S10PV and one section of separation semicoke S10PL are separated from being one section；

The cyclone separator that gas solid separation section S10 is used, the upper space being arranged in the settler R20E described in step (3) In, the hot environment of the upper space in settler R20E forms the outside high of the cyclone separator that gas solid separation section S10 is used Warm environment；

The main rotation coal gas S102V of one-level and one-level are separated into the main rotation S102 of one-level by pipeline in S102, the thick coal gas S101V that revolves Main rotation semicoke S102S；

(3) in two level pyrolytic reaction process R20, two level pyrolysis reactor R20E or settler R20E, at least a portion one are used Section separation semicoke S10PL enters two level pyrolytic reaction process R20 reaction compartment, and main body flow direction is to flow from top to bottom, is carried out Second pyrolytic reaction R20R；Two level pyrolysis char R20PS discharge two level pyrolytic reaction processes R20；

(4) in gas solid separation process S20, the dust-laden two after two level pyrolytic reaction process R20 solid powder main body bed is left Level pyrolysis coal gas R20EPV, the two of discharge gas solid separation process S20 are separated into by using the piece-rate system S20 of cyclone separator The level pyrolysis coal gas R20PV and backflow semicoke S20PS for returning to two level pyrolytic reaction space；

(5) in pipeline PP, one section of separation coal gas S10PV enters step (6) the gas solid separation section S30 by pipeline PP；

Enter the multitube parallel piece-rate system that more cyclone tubes are set in separating step S301, one section of separation coal gas S10PV, Using the lower discouraged mode of operation of discharge, discharging S301DSV under coal gas S301UV and gas-solid, discharging under gas-solid are separated into S301DSV includes semicoke S301DS and lower discouraged S301DV.

2. method according to claim 1, it is characterised in that：

Enter the multitube parallel piece-rate system that more cyclone tubes are set in separating step S301, one section of separation coal gas S10PV, Using the lower discouraged mode of operation of discharge, discharging S301DSV under coal gas S301UV and gas-solid, discharging under gas-solid are separated into S301DSV includes semicoke S301DS and lower discouraged S301DV；

Discharging S301DSV enters the piece-rate system for setting cyclone tube under separating step S302, gas-solid, using being let out under discharge The mode of operation of gas, discharging S302DSV under coal gas S302UV and gas-solid is separated into, discharging S302DSV includes semicoke under gas-solid S302DS and lower discouraged S302DV；

In semicoke storage tank V3022, discharging S302DSV is separated into coal gas V3022V and semicoke V3022S, coal gas V3022V under gas-solid From top let-down vessel V3022, semicoke V3022S is from bottom let-down vessel V3022.

3. method according to claim 1, it is characterised in that：

Enter the multitube of more guide vane formula cyclone tubes of setting simultaneously in separating step S301, one section of separation coal gas S10PV Join piece-rate system.

4. method according to claim 2, it is characterised in that：

Enter the multitube of more guide vane formula cyclone tubes of setting simultaneously in separating step S301, one section of separation coal gas S10PV Join piece-rate system；

Discharging S301DSV enters the piece-rate system for setting guide vane formula cyclone tube under separating step S302, gas-solid,

The separator S302E that the separator S301E that separating step S301 is used and separating step S302 is used is in an equipment shell Upper and lower in body S30E to be longitudinally arranged, S301E is located on S302E；

5. method according to claim 1, it is characterised in that：

(2) in gas solid separation section S10, cyclonic separation step S101, S102, S103 of 3 grades of serial operations are included；

In S103, the main rotation coal gas S102V of one-level by pipeline into the main rotation S103 of two level be separated into the main rotation coal gas S103V of two level and The main rotation semicoke S103S of two level；

One section of separation semicoke S10PL includes thick rotation semicoke S101S, the main rotation semicoke S102S of one-level and the main rotation semicoke S103S of two level；

6. method according to claim 5, it is characterised in that：

(2) in gas solid separation section S10, cyclonic separation step S101, S102, S103, S104 of 4 grades of serial operations are included；

In S104, the main rotation coal gas S103V of two level by pipeline into the main rotation S104 of three-level be separated into the main rotation coal gas S104V of three-level and The main rotation semicoke S104S of three-level；

One section of separation semicoke S10PL include thick rotation semicoke S101S, the main rotation semicoke S102S of one-level, the main rotation semicoke S103S of two level and The main rotation semicoke S104S of three-level；

7. method according to claim 3, it is characterised in that：

The coal gas S301UV of separating step S301 discharges, air-liquid separation is carried out into separation and recovery step S700.

8. method according to claim 3, it is characterised in that：

The coal gas S301UV of separating step S301 discharges, enter promoting the circulation of qi, oil, water separation into separation and recovery step S700.

9. method according to claim 3, it is characterised in that：

The coal gas S301UV of separating step S301 discharges, carried out into separation and recovery step S700 using washing fractionating column ST700 Air-liquid separates.

10. method according to claim 3, it is characterised in that：

The coal gas S302UV of separating step S302 discharges, air-liquid separation is carried out into separation and recovery step S800.

11. method according to claim 3, it is characterised in that：

The coal gas S302UV of separating step S302 discharges, enter promoting the circulation of qi, oil, water separation into separation and recovery step S800.

12. method according to claim 3, it is characterised in that：

The coal gas S302UV of separating step S302 discharges, carried out into separation and recovery step S800 using washing fractionating column ST800 Air-liquid separates.

13. method according to claim 1, it is characterised in that：

(1) in one-level pyrolytic reaction process R10, the particle diameter of the powder R10FS containing carbon hydrogen element is 0~6 millimeter, containing carbon hydrogen element One or more of the powder R10FS in following materials：

1. low rotten fine coal；

2. high rotten fine coal；

3. oil shale powder；

14. method according to claim 1, it is characterised in that：

(1) in one-level pyrolytic reaction process R10, the particle diameter of the powder R10FS containing carbon hydrogen element is 0~2 millimeter.

15. method according to claim 1, it is characterised in that：

(1) one-level pyrolytic reaction process R10 operating pressure is：0.1~6.0MPa, with absolute manometer.

16. method according to claim 1, it is characterised in that：

(1) in one-level pyrolytic reaction process R10, the powder R10FS containing carbon hydrogen element is fine coal；

One-level pyrolytic reaction process R10 reacting product outlet temperature is that one-level pyrolytic reaction process cessation reaction temperature is 350 ~700 DEG C.

17. method according to claim 1, it is characterised in that：

One-level pyrolytic reaction process R10 reacting product outlet temperature is that one-level pyrolytic reaction process cessation reaction temperature is 400 ~600 DEG C.

18. method according to claim 1, it is characterised in that：

One-level pyrolytic reaction process R10 reacting product outlet temperature is that one-level pyrolytic reaction process cessation reaction temperature is 420 ~500 DEG C.

19. method according to claim 1, it is characterised in that：

(5) in pipeline PP, one section of separation coal gas S10PV and high temperature concurrent heating gas VT100 enters step after being mixed into gaseous mixture XV (6) operation temperature of gas solid separation the section S30, XV are higher than the logistics XV dew-point temperatures of itself.

20. according to claim 19 methods described, it is characterised in that：

(5) in pipeline PP, one section of separation coal gas S10PV and high temperature concurrent heating gas VT100 enters step after being mixed into gaseous mixture XV (6) operation temperature of gas solid separation the section S30, XV are higher than XV higher than the logistics XV dew-point temperatures of itself, XV operation temperature At least 1~10 DEG C of itself dew-point temperature.

21. according to claim 19 methods described, it is characterised in that：

(5) in pipeline PP, high temperature concurrent heating gas VT100 temperature, 50~300 DEG C of coal gas S13V temperature is separated higher than three-level.

22. according to claim 19 methods described, it is characterised in that：

(5) in pipeline PP, high temperature concurrent heating gas VT100 standard state volume flow is one section of separation coal gas S10PV standard state The 5~25% of volume flow, higher than one section at least 5~20 DEG C of separation coal gas S10PV operation temperature of gaseous mixture XV operation temperatures.

23. according to claim 19 methods described, it is characterised in that：

(5) in pipeline PP, the volumetric concentration of carbon four and its above hydrocarbon component is not more than 0.05% in high temperature concurrent heating gas VT100.

24. according to claim 19 methods described, it is characterised in that：

(5) in pipeline PP, coal gas after deoiling treatments of at least a portion high temperature concurrent heating gas VT100 from coal gas S301UV, structure Into circulation logistics.

25. method according to claim 1, it is characterised in that：

(3) two level pyrolytic reaction process is entered in two level pyrolytic reaction process R20, one section of separation semicoke S10PL of at least a portion R20 reaction compartment, main body flow direction is to flow from top to bottom, and generation heating effect is contacted with the gas stripping gas V22V flowed from bottom to top The second pyrolytic reaction R20R should be carried out；Two level pyrolysis char R20PS discharge two level pyrolytic reaction processes R20；

(4) in gas solid separation process S20, the pyrolysis coal gas R20EPV of the dust-laden two level after solid powder main body bed is left, is passed through At least gas solid separation, the pyrolysis of gained dedirt two level are completed using the gas solid separation system S20 of the cyclone separator of 2 grades of serial operations Coal gas R20PV discharge gas solid separation processes S20, S20 and S10 are at least partly shared.

26. according to claim 25 methods described, it is characterised in that：

(3) in two level pyrolytic reaction process R20, two level pyrolytic reaction process R20 Gas-particle Flows status and appearance is particulate fluidization Bed.

27. method according to claim 1, it is characterised in that：

(7) course of reaction R50 being burnt in fluidisation, the semicoke based on two level pyrolysis char R20PS burns reaction compartment into fluidisation, Contacted with the oxygen-containing gas flowed from bottom to top, fluid bed occurs and burns reaction R50R, produces high-temperature oxydation semicoke R50PS and cigarette Gas YQ, flue gas YQ burn course of reaction R50 from upper space discharge fluidisation；High-temperature oxydation semicoke R50PS discharges fluidisation is burnt instead Answer process R50.

28. according to claim 27 methods described, it is characterised in that：

(7) course of reaction R50 is burnt in fluidisation, fluidizes ash-laden gas R50E- in the device for the top dilute phase section for burning reaction compartment YQ, the cyclone separation system S5 dedirts that reactor R50E internal upper parts space is burnt by being arranged in fluidisation are separated into flue gas YQ and returned Flow semicoke dust R50E-RS；Flue gas YQ, which leaves cyclone separation system S5 and discharges fluidisation, burns reactor R50E.

29. according to claim 27 methods described, it is characterised in that：

(7) course of reaction R50 is burnt in fluidisation, fluidizes ash-laden gas R50E- in the device for the top dilute phase section for burning reaction compartment YQ, the cyclone separation system S5 dedirts for the upper space for burning inside reactor by being arranged in fluidisation are separated into flue gas YQ and half Coke powder dirt R50E-RS；The semicoke dust R50E-RS of cyclone separation system S5 cyclone dip-leg discharge returns to fluidisation and burnt Reaction compartment cyclic process.

30. according to claim 27 methods described, it is characterised in that：

(7) course of reaction R50 is burnt in fluidisation, at least a portion high-temperature oxydation semicoke R50PS is as the first solid thermal carriers R10KS is used.

31. according to claim 27 methods described, it is characterised in that：

(6) course of reaction R50 is burnt in fluidisation, external warmer R50-OUT-HX is set, discharge fluidisation burns course of reaction R50's After thermal oxide semicoke enters external warmer R50-OUT-HX and takes thermal medium indirect heat exchange to reduce temperature, external warmer R30- is discharged OUT-HX。

32. according to claim 27 methods described, it is characterised in that：

(7) course of reaction R50 is burnt in fluidisation, external warmer R50-OUT-HX is set, carrys out self-fluidized type and burns course of reaction R50's Thermal oxide semicoke enters external warmer R50-OUT-HX and takes thermal medium indirect heat exchange to reduce temperature, discharge external warmer R50- OUT-HX cooling oxidation semicoke returns to fluidisation and burns course of reaction R50 recyclings.

33. according to claim 27 methods described, it is characterised in that：

(5) in pipeline PP, one section of separation coal gas S10PV and high temperature concurrent heating gas VT100 enters step after being mixed into gaseous mixture XV (6) operation temperature of gas solid separation the section S30, XV are higher than the logistics XV dew-point temperatures of itself；

At least a portion high temperature concurrent heating gas VT100 is the gas after fluidisation burns course of reaction R50 indirectly heats.

34. according to claim 33 methods described, it is characterised in that：

At least a portion high temperature concurrent heating gas VT100 is to fluidize the gas after burning course of reaction R50 indirectly heats, high temperature concurrent heating Gas VT100 media are coal gas after purification.

35. according to claim 33 methods described, it is characterised in that：

(3) it is that fluidisation is burnt dilute phase space in reactor R50E devices and arranged in two level pyrolytic reaction process R20, gas stripping gas V22V Indirect heat exchanger R50-HX discharges take hot gas.

36. according to claim 33 methods described, it is characterised in that：

(3) it is the outside semicoke heat exchanger row that fluidisation burns reactor RS0E in two level pyrolytic reaction process R20, gas stripping gas V22V What is gone out takes hot gas.

37. method according to claim 1, it is characterised in that：

In semicoke storage tank V3022, discharging S302DSV is separated into coal gas V3022V and semicoke V3022S, coal gas V3022V under gas-solid From top let-down vessel V3022, semicoke V3022S is from bottom let-down vessel V3022；

Discouraged S301DV standard state volume flow RK down, one section of standard state volume for separating coal gas S10PV is fed with S30 The ratio between flow RO is defined as K, i.e. K=RK/RO, and K values are 0.2%~10%.

38. according to claim 36 methods described, it is characterised in that：

(6) it is 1.0%~5.0% in gas solid separation section S30, K value.

39. according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 or 17 Or 18 or 19 or 20 or 21 or 22 or 23 or 24 or 25 or 26 or 27 or 28 or 29 or 30 or 31 or 32 or 33 or 34 or 35 or 36 Or 37 or 38 methods described, it is characterised in that：

(1) in one-level pyrolytic reaction process R10, the powder R10FS containing carbon hydrogen element is fine coal, and pulverized coal particle size is 0~6 millimeter；

One-level pyrolytic reaction process R10, using riser fluidized bed pyrolysis reactor, the first solid thermal carriers R10KS be from Fluidisation burns course of reaction R50 high-temperature oxydation semicoke；

One-level pyrolytic reaction process R10 reaction time is 0.1~10s, and riser reacting product outlet temperature is one-level pyrolysis Course of reaction cessation reaction temperature is 400~500 DEG C；

(3) in two level pyrolytic reaction process R20 reaction compartment, 2~12 secondary herringbone baffle plates or ring baffle, two level pyrolysis are set The temperature of the main pyrolysis section of course of reaction is 460~700 DEG C；

Two level pyrolysis section bottom is passed through 450~650 DEG C of gas stripping gas V22V and carries out tar steam stripping, and gas stripping gas V22V passes through semicoke Flow up after the bed of material and be pyrolyzed into two level pyrolytic reaction process R20 two level in coal gas product；

(4) in gas solid separation process S20, two level pyrolysis coal gas product is by between gas solid separation process S10 thick rotation and main rotation All gaps open two level pyrolytic reaction space into main whiz, main medial rotation and one-level pyrolysis coal gas be mixed into row gas solid separation；

40. according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 or 17 Or 18 or 19 or 20 or 21 or 22 or 23 or 24 or 25 or 26 or 27 or 28 or 29 or 30 or 31 or 32 or 33 or 34 or 35 or 36 Or 37 or 38 methods described, it is characterised in that：

(1) in one-level pyrolytic reaction process R10, the powder R10FS containing carbon hydrogen element is low rotten fine coal, and pulverized coal particle size is 0~6 Millimeter；

One-level pyrolytic reaction process R10 reaction time is 1.0~6s, and riser reacting product outlet temperature is that one-level pyrolysis is anti- It is 430~470 DEG C to answer process cessation reaction temperature；

(3) in two level pyrolytic reaction process R20 reaction compartment, 2~12 secondary herringbone baffle plates or ring baffle, two level pyrolysis are set The temperature of the main pyrolysis section of course of reaction is 480~600 DEG C；

(4) slightly revolved in gas solid separation process S20, two level pyrolysis coal gas product by gas solid separation process S10 between main rotation All gaps enter top whiz and open two level pyrolytic reaction space, and row gas solid separation is mixed into top medial rotation and one-level pyrolysis coal gas；

(5) in pipeline PP, one section of separation coal gas S10PV and high temperature concurrent heating gas VT100 enters step after being mixed into gaseous mixture XV (6) operation temperature of gas solid separation the section S30, XV are higher than the dew-point temperature of any component：

41. according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 or 17 Or 18 or 19 or 20 or 21 or 22 or 23 or 24 or 25 or 26 or 27 or 28 or 29 or 30 or 31 or 32 or 33 or 34 or 35 or 36 Or 37 or 38 methods described, it is characterised in that：

(1) in one-level pyrolytic reaction process R10, the R10FS of powder containing carbon hydrogen element is the low rotten fine coal of high volatile, fine coal grain Spend for 0~2 millimeter；

One-level pyrolytic reaction process R10 reaction time is 2.5~4s, and riser reacting product outlet temperature is that one-level pyrolysis is anti- It is 440~460 DEG C to answer process cessation reaction temperature；

(3) in two level pyrolytic reaction process R20 reaction compartment, 2~12 secondary herringbone baffle plates or ring baffle, two level pyrolysis are set The temperature of the main pyrolysis section of course of reaction is 480~530 DEG C；

(5) in pipeline PP, one section of separation coal gas S10PV and high temperature concurrent heating gas VT100 enters step after being mixed into gaseous mixture XV (6) operation temperature of gas solid separation the section S30, XV are higher than the dew-point temperature of any component；

42. according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 or 17 Or 18 or 19 or 20 or 21 or 22 or 23 or 24 or 25 or 26 or 27 or 28 or 29 or 30 or 31 or 32 or 33 or 34 or 35 or 36 Or 37 or 38 methods described, it is characterised in that：

The riser fluidized bed pyrolysis reactor R10E that one-level pyrolytic reaction process R10 is used and two level pyrolytic reaction process R20 The two level fluidized bed pyrolysis reactor R20E used, form unit equipment.

43. according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 or 17 Or 18 or 19 or 20 or 21 or 22 or 23 or 24 or 25 or 26 or 27 or 28 or 29 or 30 or 31 or 32 or 33 or 34 or 35 or 36 Or 37 or 38 methods described, it is characterised in that：

The two level fluidized bed pyrolysis reactor R20E that two level pyrolytic reaction process R20 is used burns course of reaction R50 with fluidisation to be made Fluid bed burns reactor R50E, forms unit equipment.

44. according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 or 17 Or 18 or 19 or 20 or 21 or 22 or 23 or 24 or 25 or 26 or 27 or 28 or 29 or 30 or 31 or 32 or 33 or 34 or 35 or 36 Or 37 or 38 methods described, it is characterised in that：

Riser fluidized bed pyrolysis reactor R10E, the two level pyrolytic reaction process R20 that one-level pyrolytic reaction process R10 is used make Two level fluidized bed pyrolysis reactor R20E, fluidisation burn the fluid bed that course of reaction R50 is used and burn reactor R50E, group Into unit equipment.

45. according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 or 17 Or 18 or 19 or 20 or 21 or 22 or 23 or 24 or 25 or 26 or 27 or 28 or 29 or 30 or 31 or 32 or 33 or 34 or 35 or 36 Or 37 or 38 methods described, it is characterised in that：

The two level fluidized bed pyrolysis reactor R20E that two level pyrolytic reaction process R20 is used, fluidisation burn course of reaction R50 uses Fluid bed to burn reactor R50E be vertical equipment, from locus, absolute altitude is said, its mutual alignment relation is：Fluid bed burns Burnt reactor R50E bottom is lower than settler R20E bottom, and the final pyrolysis char of settler R20E discharges relies on material position Difference flows into the bottom that fluid bed burns reactor R50E.

46. according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 or 17 Or 18 or 19 or 20 or 21 or 22 or 23 or 24 or 25 or 26 or 27 or 28 or 29 or 30 or 31 or 32 or 33 or 34 or 35 or 36 Or 37 or 38 methods described, it is characterised in that：

The two level fluidized bed pyrolysis reactor R20E that two level pyrolytic reaction process R20 is used, burning course of reaction R50 with fluidisation makes Fluid bed burns reactor R50E composition coaxial-type unit equipments；

It is coaxial-type Vertical Combination equipment that coaxial-type, which refers to that settler R20E, fluid bed burn reactor R50E, from space bit The relation of putting says that its mutual alignment relation is：Fluid bed surrounds settler R20E's with burning reactor R50E space segment Space；The pyrolysis char of bottom space from settler R20E flows into fluid bed by standpipe and plug valve and burns reactor R50E Lower space.

47. according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 or 16 or 17 Or 18 or 19 or 20 or 21 or 22 or 23 or 24 or 25 or 26 or 27 or 28 or 29 or 30 or 31 or 32 or 33 or 34 or 35 or 36 Or 37 or 38 methods described, it is characterised in that：