CN105462618B - A kind of hydrogasification stove, hydrogasification system and hydro-gasification process - Google Patents
A kind of hydrogasification stove, hydrogasification system and hydro-gasification process Download PDFInfo
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- CN105462618B CN105462618B CN201510893654.6A CN201510893654A CN105462618B CN 105462618 B CN105462618 B CN 105462618B CN 201510893654 A CN201510893654 A CN 201510893654A CN 105462618 B CN105462618 B CN 105462618B
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Abstract
The invention discloses a kind of hydrogasification stove, hydrogasification system and hydro-gasification process, it is related to Coal Gasification Technology field, for realizing simple, the efficient utilization to tar.The hydrogasification stove includes outer barrel and the inner cylinder in the outer barrel, the inner cylinder includes interconnected reative cell and chill zone, the reative cell is located above the chill zone, syngas outlet is provided with the outer barrel, the syngas outlet is located at below the junction of the reative cell and the chill zone, the hydrogasification stove also includes the chiller positioned at the junction of the reative cell and chill zone periphery, tar has been passed through in the chiller, multiple first jets towards the bottom of the reative cell are provided with the chiller, it is provided with the bottom of the reative cell and the one-to-one multiple first tar holes of first jet.The present invention is used to carry out hydrogasification processing to coal.
Description
Technical field
The present invention relates to Coal Gasification Technology field, more particularly to a kind of hydrogasification stove, hydrogasification system and hydrogenation
Change method.
Background technology
China is a rich coal, the country of oil-poor, few gas, and with the rapid development of China's economy, to oil and naturally
The demand of gas is more and more, therefore, how coal is reasonably utilized, to reduce the demand to oil and natural gas,
As a main direction of development of China's coal technical field.
At present, mainly coal is utilized by coal chemical technology, specifically, coal chemical industry refers to using coal as raw material, through changing
Learn the process that processing makes coal be converted into gas, liquid, solid fuel etc..Coal chemical technology includes coking, low temperature distillation and hydrogenation
Gasification etc., wherein, after coking, low temperature distillation or hydrogasification processing are carried out to coal, target product can be not only obtained, can also be produced
Go out tar.If tar is directly discarded, enterprise profit can be reduced, endanger environment, therefore this part tar is re-used into tool
It is of great significance.
In the prior art, the re-using to tar mainly is realized by using the mode of Tar production light-end products, led to
Often, included using the mode of Tar production light-end products following two：Hydrogenation of tar refines and coal tar deep processing technique.Its
In, it is necessary to first carry out certain pretreatment to tar in hydrogenation of tar subtractive process, and need catalyst and higher pressure strip
Part (13MPa~15MPa), process complicated difficult are realized；And in coal tar deep processing technical process, the oil product of acquisition is higher with boiling point
Tar heavy oil based on, fail to realize efficient utilization to tar.
The content of the invention
It is an object of the invention to provide a kind of hydrogasification stove, hydrogasification system and hydro-gasification process, for reality
Now to simple, the efficient utilization of tar.
To reach above-mentioned purpose, the present invention provides a kind of hydrogasification stove, adopted the following technical scheme that：
The hydrogasification stove includes outer barrel and the inner cylinder in the outer barrel, and the inner cylinder includes interconnected reaction
Room and chill zone, the reative cell are located on the chill zone, syngas outlet are provided with the outer barrel, the synthesis gas goes out
Mouthful below the junction of the reative cell and the chill zone, the hydrogasification stove also include positioned at the reative cell and
The chiller of the junction periphery of the chill zone, has been passed through tar in the chiller, direction is provided with the chiller
Multiple first jets of the bottom of the reative cell, it is provided with first jet one by one on the bottom of the reative cell
Corresponding multiple first tar holes.
The invention provides a kind of hydrogasification stove as described above, because the hydrogasification stove also includes being located at reative cell
With the chiller of the junction of chill zone periphery, multiple first jets of the bottom of orientating reaction room are provided with chiller,
Be provided with the bottom of reative cell with the one-to-one multiple first tar holes of the first jet so that using hydrogenation
During changing stove to coal progress hydrogasification processing, chiller can spray tar into reative cell, and then cause the portion
Divide tar to carry out hydrogasification reaction in the reaction chamber, light-end products are generated, without to hydrogasification of the prior art
The structure and hydro-gasification process of stove carry out big change, you can by tar conversion be light-end products, focused therefore, it is possible to realize
Simple, the efficient utilization of oil.
Further, the invention provides a kind of hydrogasification system, the hydrogasification system includes above-described add
Hydrogen gasification furnace, the first tar transmission pipeline and after-treatment system, wherein, the after-treatment system connects with the syngas outlet
Logical, one end of the first tar transmission pipeline connects with the after-treatment system, and the other end connects with the chiller, is used for
The tar that the after-treatment system obtains is delivered in the chiller.Because the hydrogasification system is including above-described
Hydrogasification stove, therefore, the hydrogasification system has and above-described hydrogasification stove identical beneficial effect, herein not
Repeated again.
In addition, present invention also offers a kind of hydro-gasification process, coal is carried out using above-described hydrogasification stove
Hydrogasification is handled, and the hydro-gasification process includes：Using the chiller tar is sprayed into the reative cell；Into described
Hydrogasification reaction generation light-end products occur in the reative cell for the tar in reative cell.
The invention provides a kind of hydro-gasification process as described above, coal is added using the hydro-gasification process
During hydrogen gasification process, tar is sprayed into reative cell using chiller, can reacted into the tar in reative cell
Hydrogasification reaction generation light-end products occur in room, it is therefore not necessary to the structure of hydrogasification stove of the prior art and plus
Hydrogen gasification process carries out big change, you can by tar conversion is light-end products, and then realizes simple, the efficient profit to tar
With.
Brief description of the drawings
In order to illustrate more clearly about the embodiment of the present invention or technical scheme of the prior art, embodiment will be described below
In the required accompanying drawing used be briefly described, it should be apparent that, drawings in the following description be only the present invention some
Embodiment, for those of ordinary skill in the art, on the premise of not paying creative work, can also be attached according to these
Figure obtains other accompanying drawings.
Fig. 1 is the schematic diagram of the hydrogasification stove in the embodiment of the present invention；
Fig. 2 is the Longitudinal cross section schematic of the chiller position in the embodiment of the present invention；
Fig. 3 is the cross-sectional view of the chiller position in the embodiment of the present invention；
Fig. 4 is the schematic diagram of the hydrogasification system in the embodiment of the present invention；
Fig. 5 is the flow chart of the hydro-gasification process in the embodiment of the present invention.
Description of reference numerals：
1-outer barrel；11-syngas outlet；2-inner cylinder；
21-reative cell；22-chill zone；23-junction；
3-chiller；4-main tar pipeline；5-short tube；
6-conical baffle；7-ring baffle plate；8-nozzle；
9-blowback gas port；10-hydrogasification stove；
20-the first tar transmission pipeline；30-after-treatment system；
40-the second tar transmission pipeline；50-outside tar source.
Embodiment
Below in conjunction with the accompanying drawing in the embodiment of the present invention, the technical scheme in the embodiment of the present invention is carried out clear, complete
Site preparation describes, it is clear that described embodiment is part of the embodiment of the present invention, rather than whole embodiments.Based on this hair
Embodiment in bright, the every other implementation that those of ordinary skill in the art are obtained under the premise of creative work is not made
Example, belongs to the scope of protection of the invention.
Embodiment one
As shown in figure 1, hydrogasification stove provided in an embodiment of the present invention includes outer barrel 1 and the inner cylinder 2 in outer barrel 1,
Inner cylinder 2 includes interconnected reative cell 21 and chill zone 22, and reative cell 21 is located at the top of chill zone 22, is provided with outer barrel 1
Syngas outlet 11, syngas outlet 11 are located at the lower section of junction 23 of reative cell 21 and chill zone 22.Further, hydrogenation
Changing stove also includes the chiller 3 of the periphery of junction 23 positioned at reative cell 21 and chill zone 22, and tar has been passed through in chiller 3,
Multiple first jets of the bottom of orientating reaction room 21 are provided with chiller 3, are provided with the bottom of reative cell 21 and the
The one-to-one multiple first tar holes of one jet, so that carrying out hydrogasification processing to coal using hydrogasification stove
During, chiller 3 can spray tar into reative cell 21, and then enable the part tar in reative cell 21
Generation hydrogasification is reacted, and light-end products is generated, without the structure to hydrogasification stove of the prior art and hydrogasification side
Method carries out big change, you can by tar conversion is light-end products, therefore, it is possible to realize simple, the efficient utilization to tar.Separately
Outside, the part tar can also to the synthesis gas in reative cell 21, (i.e. hydrogasification occurs in reative cell 21 for coal dust anti-simultaneously
The synthesis gas that should be generated) play a part of Quench, without again by media such as gas or water to the synthesis gas in reative cell 21
Quench is carried out, is advantageous to save energy consumption and reduces the output of waste gas or waste water.
Alternatively, the length of inner cylinder 2 is the 1/3~3/5 of the length of whole outer barrel 1.Set and protect between inner cylinder 2 and outer barrel 1
Warm layer, heat-insulation layer is interior to be filled with insulation material, to prevent inner cylinder 2 and extraneous heat exchange.Exemplarily, insulation material is stone
Ying Mian.
Further, it is preferred in the embodiment of the present invention, as shown in figure 1, the junction 23 of reative cell 21 and chill zone 22
Diameter is less than the diameter (in Fig. 1 shown in D) of inner cylinder 2, in shrink mouth shape, i.e., along the direction for moving closer to chill zone 22, reative cell 21
The diameter of bottom be gradually reduced, along the direction for moving closer to reative cell 21, the diameter at the top of chill zone 22 is gradually reduced.By
There is said structure in junction 23, so that synthesis gas is during junction 23 is flowed through, after its flow velocity can first increase
Reduce (integrally showing the increased effect of flow velocity) so that the flow field of synthesis gas changes, and the semicoke in synthesis gas by
Cause change in flow slightly slower than synthesis gas in inertia reason, so that there is gap in terms of speed in synthesis gas and semicoke, it is real
Show synthesis gas and be mixed into the first separation of semicoke therein, reduce the dustiness of synthesis gas.Alternatively, the diameter of junction 23
For the 2/5~4/5 of the diameter of inner cylinder 2.Angle between the side wall and horizontal direction of the bottom of reative cell 21 is 30 °~60 °, is swashed
Angle between the side wall and horizontal direction at the top of cold-zone 22 is also 30 °~60 °, and the two can be the same or different.
In addition, multiple towards the top of chill zone 22 are also provided with chiller 3 in the embodiment of the present invention
Two jets, be provided with the top of chill zone 22 with the one-to-one multiple second tar holes of the second jet so that
Tar can be sprayed into chill zone 22 by chiller 3, to carry out Quench to the synthesis gas in chill zone 22, without passing through again
The medium such as gas or water carries out Quench to the synthesis gas in chill zone 21, be advantageous to further to save energy consumption and reduction waste gas or
The output of person's waste water, and part tar can also occur hydrogasification reaction and be changed into light-end products, further improve burnt
The utilization rate of oil.
Exemplarily, the concrete structure of chiller 3 can be it is following two, the first, as shown in Figures 2 and 3, chiller
3 include a ring pipe, and ring pipe connects with main tar pipeline 4, wherein, one is provided with ring pipe and ranked first jet and one
It ranked second jet；Second, chiller 3 includes two ring pipes setting up and down, two ring pipes with main tar pipeline 4
Connection, wherein, one is provided with the ring pipe of top setting and ranked first jet, a row is provided with the ring pipe set on the lower
Second jet.Pump can be connected with main tar pipeline 4, to provide power for tar, tar is flowed in ring pipe
It is dynamic smooth.
For the chiller 3 of above two structure, the first jet or the second jet on ring pipe can be with
It is uniformly distributed on whole ring pipe, the number of the number of the first jet and the second jet can be the same or different,
Correspondingly, the first tar hole on the bottom of reative cell 21 or the second tar hole on the top of chill zone 22 can also
It is uniformly distributed, the number in the number in the first tar hole and the second tar hole can be the same or different.
Wherein, when chiller 3 has the first structure, the structure of chiller 3 is simple.When chiller 3 has second
During structure, the amount for being capable of the tar to being spurted into by chiller 3 in reative cell 21 and chill zone 22 respectively is controlled, favorably
In being more accurately controlled to the temperature in reative cell 21 and chill zone 22, for example, two can be set in hydrogasification stove
The auxiliary tar pipeline of bar, wherein, one end of every auxiliary tar pipeline connects with a ring pipe, and the other end connects with main tar pipeline 4
It is logical, and valve is provided with two auxiliary tar pipelines, and then can be by control valve to spurting into reaction by chiller 3
The amount of room 21 and the tar in chill zone 22 is accurately controlled.
Certainly, the concrete structure of chiller 3 is not limited to both the above, no longer repeats one by one herein, art technology
Personnel can be configured according to being actually needed to the concrete structure of chiller 3.
Implement for the ease of those skilled in the art, the chiller 3 with above two concrete structure is included below
The details of ring pipe is described in detail：
Alternatively, above-mentioned ring pipe is annular pipe, and the caliber of annular pipe needs to be more than 2cm, to ensure annular pipe
In there is the tar of sufficient amount, and the blocking of annular pipe can be prevented.Exemplarily, the caliber of annular pipe is inner cylinder 2
The 1/10~1/20 of diameter.
Alternatively, the first jet, the second jet, the first tar hole and the shape in the second tar hole are circle, are shown
Example property, the first jet, the second jet, the first tar hole and the diameter in the second tar hole are the caliber of annular pipe
3/10~7/10, so as to the tar of sufficient amount can be sprayed into reative cell 21 and chill zone 22 by annular pipe, and can be with
Prevent the blocking in above-mentioned each jet and hole.
If in addition, when chiller 3 only includes a ring pipe, if the diameter of the second jet is more than first on ring pipe
The diameter of jet, because the second injection mouth down is set, so that a large amount of tar can eject from the second jet, cause
Tar is difficult to project into reative cell 21 from the first jet, and the utilization rate of tar is not high, therefore, the second injection on ring pipe
The diameter of mouth should be not more than the diameter of the first jet, larger to have when enabling tar to be ejected from the second jet
Resistance, and then reduce tar and the utilization rate that to the difficulty in reative cell 21, ensure that tar is projected from the first jet.
In addition, preferably as shown in Fig. 2 passing through short tube 5 between the first jet and the first tar hole in the embodiment of the present invention
Connection, is connected between the second jet and the second tar hole also by short tube 5, to enable the tar that is sprayed from ring pipe
Fully enter in reative cell 21 and chill zone 22, and ring pipe can also be fixed on by short tube 5 on the barrel of inner cylinder 2,
Maintain the stabilization of the structure of hydrogasification stove.Alternatively, the length of short tube 5 is 1cm~3cm.
You need to add is that as shown in figure 1, the hydrogasification stove in the embodiment of the present invention also includes the bottom with chill zone 22
The conical baffle 6 of portion's connection, the bottom of conical baffle 6 have a circular open, and along vertically downward direction, conical baffle
The diameter of 6 cross section is gradually reduced.Because conical baffle 6 has structure as described above, so that in chill zone 22
Synthesis gas after the outflow of the circular open of the bottom of conical baffle 6, flow up and rapid spatial expansion, and then cause synthesis
The flowing velocity of gas reduces rapidly, can realize further separating for synthesis gas and semicoke.Alternatively, the side of conical baffle 6
Angle between wall and vertical direction is 15 °~30 °, to cause the setting of conical baffle 6 will not be to reative cell 21 and Quench
Pressure and flow field in area 22 etc. produce harmful effect, are advantageous to being smoothed out for coal hydrogenation gasification reaction.
In addition, as shown in figure 1, it is also provided with ring on the outer barrel 1 that the hydrogasification stove in the embodiment of the present invention includes
Shape deflection plate 7, ring baffle plate 7 is located at the lower section of syngas outlet 11, so that synthesis gas flows out from syngas outlet 11
Before, ring baffle plate 7 can be first passed through, because ring baffle plate 7 has baffling effect to synthesis gas, so as to realize synthesis
Gas and semicoke continue to separate.
It should be noted that when hydrogasification stove includes above-mentioned conical baffle 6 and ring baffle plate 7 simultaneously, annular
Deflection plate 7 needs to match with conical baffle 6, further to improve the separating effect of synthesis gas and semicoke.Exemplarily, circle
When angle between conical baffled 6 side wall and vertical direction is 15 °~30 °, between the barrel of ring baffle plate 7 and outer barrel 1
Angle be 30 °~60 °.
In addition, as shown in figure 1, the hydrogasification stove in the embodiment of the present invention can also include stretching into from the top of outer barrel 1
Coal dust pipeline and hydrogen gas lines and the nozzle 8 positioned at the top of inner cylinder 2, alternatively, nozzle 8 includes two passages, wherein one
Individual passage connects coal dust pipeline, and another passage connection hydrogen gas lines, certainly, nozzle 8 can also include multiple passages, wherein,
The passage connection coal dust pipeline of centre, the multiple passage connection hydrogen gas lines of surrounding, so that coal dust and hydrogen are sufficiently mixed can be made
Gasification, the embodiment of the present invention is to the concrete structure of nozzle 8 without limiting.As shown in figure 1, the hydrogenation in the embodiment of the present invention
The blowback gas port 9 positioned at the bottom of hydrogasification stove can also be included by changing stove, and blowback gas port 9 is used to be passed through into hydrogasification stove
Blowback air, to loosen the semicoke positioned at the bottom of hydrogasification stove, and then prevent the semicoke pressure positioned at the bottom of hydrogasification stove
It is real, ensure that semicoke blanking is smooth.
The process for being carried out hydrogasification processing to coal using the hydrogasification stove in the embodiment of the present invention is specifically included：It is first
First, entered by the coal dust that lock hopper ships through coal dust pipeline in the passage of nozzle 8, hydrogen enters the passage of nozzle 8 through hydrogen gas lines
In, then the two through nozzle 8 mixing after enter reative cell 21 in, temperature be 850 DEG C~1000 DEG C, pressure be 5MPa~
Under conditions of 10MPa, coal dust reacts with hydrogen, and generation synthesis gas, oil product and semicoke, oil product herein is gaseous state, including
25%~45% tar heavy oil and 60%~75% tar light oil；Then, synthesis gas flows downward to the bottom of reative cell 21,
The tar spurted into chiller 3 in reative cell 21 mixes, and exchanges heat to 800 DEG C~850 DEG C rapidly, and occurs to add at such a temperature
Hydrogen gasification reaction, the predominantly hydrogasification reaction of tar herein, it is main including the fracture of bridged bond on aromatic ring, part aromatic ring plus
Hydrogen, branch chain break etc., and then be tar light oil by tar conversion；Then, synthesis gas enters in chill zone 22, and synthesis gas is swashed
The tar Quench that cooler 3 is spurted into chill zone 22, temperature are down to 780 DEG C~800 DEG C, while partial hydrogenation to occur anti-for tar
Should, bridged bond and the fracture compared with long linear carbon-carbon bond on the aromatic ring predominantly based on the endothermic reaction, with occurring in reative cell 21
Tar hydrogasification reaction compare, partial hydrogenation reaction obtain light-end products content it is slightly lower；Finally, synthesis gas passes through successively
After crossing conical baffled 6, ring baffle plate 7, flowed out from syngas outlet 11, into after-treatment system.
After carrying out hydrogasification processing to coal using hydrogasification stove of the prior art, contain 25% in the oil product of gained
~45% tar heavy oil, and after carrying out hydrogasification processing to coal by using the hydrogasification stove in the embodiment of the present invention, institute
Oil product in the content of tar heavy oil can be reduced to less than 15%, the content of triphen can be improved to 80%~90% in oil product.Cause
This, can not only be simply and efficiently right when carrying out hydrogasification processing to coal using the hydrogasification stove in the embodiment of the present invention
Tar is utilized, moreover it is possible to is effectively reduced the content of tar heavy oil in the oil product of gained, is improved and carry out hydrogasification processing to coal
Efficiency.
The embodiments of the invention provide a kind of hydrogasification stove as described above, because the hydrogasification stove also includes being located at
The chiller 3 of the periphery of junction 23 of reative cell 21 and chill zone 22, the bottom of orientating reaction room 21 is provided with chiller 3
Multiple first jets, be provided with the bottom of reative cell 21 with the one-to-one multiple first tar holes of the first jet, from
And make it that during hydrogasification processing is carried out to coal using hydrogasification stove, chiller 3 can spray tar to anti-
Answer in room 21, and then enable the part tar to carry out hydrogasification reaction in reative cell 21, generate light-end products, without
Structure to hydrogasification stove of the prior art and hydro-gasification process carry out big change, you can by tar conversion are lightweight
Oil product, therefore, it is possible to realize simple, the efficient utilization to tar.
Embodiment two
In addition, the embodiment of the present invention additionally provides a kind of hydrogasification system, as shown in figure 4, the hydrogasification system bag
Hydrogasification stove 10, the first tar transmission pipeline 20 and the after-treatment system 30 described in embodiment one are included, wherein, the post processing
System 30 connects with the syngas outlet in hydrogasification stove 10, one end and the after-treatment system 30 of the first tar transmission pipeline 20
Connection, the other end connect with the chiller in hydrogasification stove 10, and the tar for after-treatment system 30 to be obtained is delivered to sharp
In cooler.
Because the hydrogasification system includes above-described hydrogasification stove 10, therefore, the hydrogasification system has
With the above-described identical beneficial effect of hydrogasification stove 10, no longer repeated herein.Further, since in the hydrogasification
In system, the tar that after-treatment system 30 obtains can be transported in chiller, and is reused, and therefore, application is above-mentioned
When hydrogasification system carries out hydrogasification processing to coal, additionally it is possible to make the cost of coal hydrogenation gasification processing procedure relatively low.
Inventors herein have recognized that the synthesis gas of after-treatment system 30 is entered by the syngas outlet of hydrogasification stove 10
Temperature be about 750 DEG C~780 DEG C, and be wherein still mixed with semicoke, therefore, after-treatment system 30 needs to have to enter synthesis gas
The functions such as row dedusting, energy regenerating, Oil Recovery and purification.Exemplarily, the after-treatment system 30 includes dust removing units, heat exchange
Unit, separative element and clean unit etc., wherein, dust removing units can include cyclone separator and filter, and heat exchange unit can
So that one-level knockout drum and two fractions can be included including hydrogen heater and hydrogen preheater, useless pot, water cooler, separative element
From tank.Synthesis gas can pass through above unit successively, also can be alternately across above unit.
Exemplarily, the processing procedure handled in after-treatment system 30 synthesis gas is as follows：
First, the synthesis gas discharged by the syngas outlet of hydrogasification stove 10 carries out just dedusting in cyclone separator,
Whirlwind in cyclone separator can be one cyclonic or multistage cyclone, and after first dedusting, the entrainment of semicoke can be down in synthesis gas
5g/m3~15g/m3；
Then, synthesis gas enters hydrogen heater, synthesis gas is fully exchanged heat with hydrogen in hydrogen heater, after heat exchange
The temperature of synthesis gas is down to 530 DEG C~570 DEG C, and hydrogen is then preheated to 600 DEG C by 250 DEG C, then is further exchanged heat through useless pot, synthesizes
The temperature of gas can be down to 300 DEG C~330 DEG C, and give up pot then by-product superheated steam.
Synthesis gas passes through filter, is down to the entrainment of semicoke in synthesis gas under the filtration of filter element
5mg/m3~10mg/m3, i.e., refined dedusting is carried out to synthesis gas, to remove the semicoke in synthesis gas, ensures oil quality.Adopt herein
Filter can be ceramic filter or metal sintered filter.
Then, the synthesis gas after refined dedusting enters hydrogen preheater, in order to make hydrogen have preferable pre- thermal effect as far as possible
Fruit, above-mentioned hydrogen preheater can set multistage, so that hydrogen can be preheating to 250 DEG C by 30 DEG C.
Synthesis gas after fully being exchanged heat with hydrogen enters one-level knockout drum, and one-level knockout drum outlet temperature is down to 110~130
℃.After synthesis gas is separated in one-level knockout drum, tar heavy oil can be obtained, wherein, tar heavy oil using the derivatives such as naphthalene, phenanthrene as
It is main.
Finally, the synthesis gas come out by one-level knockout drum, after water cooler heat-exchange temperature is down to 40 DEG C, into two level
Knockout drum, after synthesis gas is separated in the second-order separation tank, tar light oil can be obtained, tar light oil mainly includes crude benzol, can
Directly as output of products, wherein, in water cooler can be passed through cold medium makes the temperature of synthesis gas be down to 5 DEG C or so,
Synthesis gas crude benzol amount separating obtained in the second-order separation tank can be further improved, in addition, the conjunction come out by the second-order separation tank
Still contain a certain amount of benzene vapour into gas, synthesis gas can be continued to handle in clean unit, further to collect
Crude benzol, here is omitted.
Further, the after-treatment system 30 in the embodiment of the present invention also includes indirect condensing equipment, and the first tar passes
One end of defeated pipeline 20 connects with indirect condensing equipment, and when the other end connects with chiller, indirect condensing equipment can be to by closing
The tar heavy oil isolated into gas carries out indirect condensing, because during indirect condensing, free from admixture is mixed into tar heavy oil, and still
Mobility is so kept, and then directly tar heavy oil can be delivered in chiller by the first tar transmission pipeline 20 so that this
Hydro-gasification process in inventive embodiments is simple, and cost is low.
In addition, as shown in figure 4, the hydrogasification system in the embodiment of the present invention can also include the second tar transmission pipeline
40 and outside tar source 50, wherein, one end of the second tar transmission pipeline 40 connects with outside tar source 50, the other end and Quench
Device connects, for the tar in outside tar source 50 to be delivered in chiller, with when to coal progress hydrogasification processing institute
When the amount of the tar heavy oil obtained can not meet the needs of hydrogasification stove 10, the normal operation of hydrogasification stove 10 is maintained.
Alternatively, the main tar of the first tar transmission pipeline 20 and the second tar transmission pipeline 40 with hydrogasification stove 10
Pipeline communication, so that the tar in two transmission pipelines is supplied to chiller after sufficiently mixing.Wherein, in outside tar source 50
Tar can be coking or the tar obtained by low temperature distillation.When the tar in outside tar source 50 is with phenols, hydro carbons, pitch
When alkene etc. is main, heat tracing or addition solvent need to be added to ensure mobility of the part tar in the second tar transmission pipeline 40.
In addition, valve can be equipped with the first tar transmission pipeline 20 and the second tar transmission pipeline 40, to adjust main tar pipeline
In tar amount and composition.
Coal is added in addition, the embodiment of the present invention additionally provides a kind of hydrogasification stove using described in embodiment one
The hydro-gasification process of hydrogen gasification process, as shown in figure 5, the hydro-gasification process includes：Step S501, using chiller to anti-
Answer and tar is sprayed in room；Step S502, hydrogasification reaction generation lightweight occurs in the reaction chamber into the tar in reative cell
Oil product.Wherein, step S501 and step S502 detailed content are referred to the associated description of hydrogasification stove in embodiment one,
No longer repeated herein.
Further, the hydro-gasification process in the embodiment of the present invention also includes：Sprayed using chiller into chill zone
Tar, into the tar in chill zone in chill zone synthesis gas carry out Quench the step of.Similarly, above step is detailed
Content is referred to the associated description of hydrogasification stove in embodiment one, is no longer repeated herein.
The embodiments of the invention provide a kind of hydro-gasification process as described above, is using the hydro-gasification process to coal
During carrying out hydrogasification processing, tar is sprayed into reative cell using chiller, into the tar in reative cell
Hydrogasification reaction generation light-end products occur in the reaction chamber, it is therefore not necessary to the knot to hydrogasification stove of the prior art
Structure and hydro-gasification process carry out big change, you can by tar conversion be light-end products, and then realize to tar it is simple,
Efficiently utilize.
The foregoing is only a specific embodiment of the invention, but protection scope of the present invention is not limited thereto, any
Those familiar with the art the invention discloses technical scope in, change or replacement can be readily occurred in, should all be contained
Cover within protection scope of the present invention.Therefore, protection scope of the present invention should be based on the protection scope of the described claims.
Claims (19)
1. a kind of hydrogasification stove, including outer barrel and the inner cylinder in the outer barrel, it is characterised in that the inner cylinder includes phase
Intercommunicated reative cell and chill zone, the reative cell are located above the chill zone, and being provided with synthesis gas on the outer barrel goes out
Mouthful, the syngas outlet is located at below the junction of the reative cell and the chill zone, and the hydrogasification stove also includes
Chiller positioned at the junction of the reative cell and chill zone periphery, tar is passed through in the chiller, it is described to swash
Multiple first jets towards the bottom of the reative cell are provided with cooler, are provided with the bottom of the reative cell and institute
State the one-to-one multiple first tar holes of the first jet.
2. hydrogasification stove according to claim 1, it is characterised in that be additionally provided with towards described and swash on the chiller
Multiple second jets at the top of cold-zone, it is provided with the top of the chill zone one-to-one with second jet
Multiple second tar holes.
3. hydrogasification stove according to claim 2, it is characterised in that the chiller includes a ring pipe, described
Ring pipe and main tar pipeline communication, wherein, the is provided with described in the first jet described in a row and a row on the ring pipe
Two jets.
4. hydrogasification stove according to claim 2, it is characterised in that the chiller includes two rings setting up and down
Shape pipe, two ring pipes with main tar pipeline communication, wherein, be provided with the ring pipe of top setting described in a row
One jet, the second jet described in a row is provided with the ring pipe set on the lower.
5. hydrogasification stove according to claim 4, it is characterised in that the hydrogasification stove also includes two auxiliary tar
Pipeline, one end of every auxiliary tar pipeline connect with a ring pipe, the other end with the main tar pipeline
Connect, valve is provided with two auxiliary tar pipelines.
6. the hydrogasification stove according to claim 3 or 4, it is characterised in that the ring pipe is annular pipe, the circle
The caliber of ring pipe is more than 2cm.
7. hydrogasification stove according to claim 6, it is characterised in that the caliber of the annular pipe is the inner cylinder
The 1/10~1/20 of diameter.
8. hydrogasification stove according to claim 6, it is characterised in that first jet, second jet,
The shape in the first tar hole and the second tar hole is circle, first jet, second jet, institute
The diameter for stating the first tar hole and the second tar hole is the 3/10~7/10 of the caliber of the annular pipe.
9. the hydrogasification stove according to claim 3 or 4, it is characterised in that first jet and first Jiao
Connected by short tube between oilhole, connected between second jet and the second tar hole also by short tube.
10. hydrogasification stove according to claim 9, it is characterised in that the length of the short tube is 1cm~3cm.
11. hydrogasification stove according to claim 1, it is characterised in that the hydrogasification stove also includes swashing with described
The conical baffle of the bottom connection of cold-zone, the conical baffled bottom have a circular open, and along vertically downward direction, institute
The diameter for stating conical baffled cross section is gradually reduced.
12. hydrogasification stove according to claim 11, it is characterised in that the conical baffled side wall and vertical direction
Between angle be 15 °~30 °.
13. hydrogasification stove according to claim 11, it is characterised in that annular baffling is additionally provided with the outer barrel
Plate, the ring baffle plate are located at below the syngas outlet.
14. hydrogasification stove according to claim 13, it is characterised in that the cylinder of the ring baffle plate and the outer barrel
Angle between wall is 30 °~60 °.
A kind of 15. hydrogasification system, it is characterised in that including the hydrogasification stove as described in any one of claim 1~14,
First tar transmission pipeline and after-treatment system, wherein, the after-treatment system connects with the syngas outlet, and described
One end of one tar transmission pipeline connects with the after-treatment system, and the other end connects with the chiller, after will be described
The tar that processing system obtains is delivered in the chiller.
16. hydrogasification system according to claim 15, it is characterised in that the after-treatment system includes indirect condensing
Equipment, one end of the first tar transmission pipeline connect with the indirect condensing equipment, and the other end connects with the chiller.
17. the hydrogasification system according to claim 15 or 16, it is characterised in that the hydrogasification system includes the
Two tar transmission pipelines and outside tar source, wherein, one end of the second tar transmission pipeline connects with the outside tar source
Logical, the other end connects with the chiller, for the tar in the outside tar source to be delivered in the chiller.
18. a kind of hydro-gasification process, it is characterised in that use the hydrogasification stove as described in any one of claim 1~14
Hydrogasification processing is carried out to coal, the hydro-gasification process includes：
Will coal dust and hydrogen mix after spray into reative cell, there is provided a temperature is 850 DEG C~1000 DEG C, pressure be 5MPa~
10MPa reaction condition, reacted under the cited reaction conditions into the coal dust in the reative cell and hydrogen, generation synthesis gas,
Gaseous oil product and semicoke；
Using the chiller tar is sprayed into the reative cell；
Exchanged heat into the tar in the reative cell and the synthesis gas to 800 DEG C~850 DEG C, and the tar 800 DEG C~
Under 850 DEG C of reaction temperature, hydrogasification reaction generation light-end products occur in the reative cell.
19. hydro-gasification process according to claim 18, it is characterised in that the hydro-gasification process also includes：
Using the chiller tar is sprayed into the chill zone；
Quench is carried out to the synthesis gas in the chill zone into the tar in the chill zone.
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| CN201510893654.6A CN105462618B (en) | 2015-12-08 | 2015-12-08 | A kind of hydrogasification stove, hydrogasification system and hydro-gasification process |
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| CN106479577A (en) * | 2016-12-06 | 2017-03-08 | 北京神雾环境能源科技集团股份有限公司 | A kind of system and method for coal sub-prime cascade utilization |
| CN106479547A (en) * | 2016-12-06 | 2017-03-08 | 神雾环保技术股份有限公司 | The system and method that a kind of coal is classified dual treatment |
| CN109251770B (en) * | 2018-11-28 | 2020-03-13 | 新奥科技发展有限公司 | Coal hydro-gasification method and hydro-gasification furnace applying same |
| CN110835553B (en) * | 2019-11-05 | 2021-06-25 | 新奥科技发展有限公司 | Hydro-gasification process |
| CN112375594B (en) * | 2020-11-17 | 2021-07-06 | 新奥科技发展有限公司 | Coal hydro-gasification reaction furnace and coal hydro-gasification reaction method |
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| US4007017A (en) * | 1975-12-22 | 1977-02-08 | Slater William L | Production of clean synthesis or fuel gas |
| CN101067092A (en) * | 2006-08-15 | 2007-11-07 | 何巨堂 | Methd of spearating lower oil in coal tar hydrogenating conversion process |
| CN101580739B (en) * | 2009-03-12 | 2013-01-09 | 徐州燃控科技股份有限公司 | Fixed bed straw gasification process with tar backflash |
| CN202744505U (en) * | 2012-09-04 | 2013-02-20 | 新奥科技发展有限公司 | Chiller and gasification furnace with same |
| CN204455014U (en) * | 2015-02-27 | 2015-07-08 | 山东宝塔新能源有限公司 | With the coal tar hydrogenating reaction unit of double-reactor |
| CN104862014B (en) * | 2015-04-28 | 2018-05-15 | 新奥科技发展有限公司 | A kind of hydrogasification stove and its hydro-gasification process |
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