CN205024184U - Piece -rate system of raw gas - Google Patents
Piece -rate system of raw gas Download PDFInfo
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- CN205024184U CN205024184U CN201520732098.XU CN201520732098U CN205024184U CN 205024184 U CN205024184 U CN 205024184U CN 201520732098 U CN201520732098 U CN 201520732098U CN 205024184 U CN205024184 U CN 205024184U
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Abstract
The utility model discloses a piece -rate system of raw gas, including the tower body, be connected with the outlet duct at the tower body top, thick gas inlet is equipped with in the lower part, and the burnt oil pipe of the row of being connected with in the bottom connects first tar shower on upper portion, be connected with on the first tar shower to stretch into the inside first tar shower nozzle that is located the below of the air inlet of outlet duct of tower body, at tower body middle part connection second tar shower, be connected with on the second tar shower and stretch into the inside second tar shower nozzle of tower body, second tar shower nozzle is located the below of first tar shower nozzle, the length at first tar shower nozzle to tower body top is the 110 -29 of tower body total length, the length at second tar shower nozzle to tower body top is the 12 -23 of tower body total length, thick gas inlet is the 23 -45 of tower body total length to the length at tower body top. The problem of oil -gas separation device structure among the prior art complicated, it is not good, with high costs with the tar effect to remove the dust, maintenance inconvenience is solved.
Description
Technical field
The utility model belongs to coal chemical technology, is specifically related to a kind of separation system of raw gas.
Background technology
China is an oil starvation, weak breath and the country of coal resources relative abundance, and coal is not also well utilized as a kind of energy of alternative rich reserves.Along with the fast development of economy, China energy demand maintains rapid growth, and the growth year by year of domestic crude oil demand, the import volume of crude oil constantly refreshes historical record, and domestic oil production rate can not meet the requirement of domestic economy high speed development far away.Therefore, greatly develop Chemical Industry, with Coal Chemical Industry products substitution petrochemicals, become the inevitable choice of China's energy strategy.
At present, the upgrading of fine coal carbonization has become a development hot topic of present stage.But because the raw material used in fine coal carbonization is fine coal, make to there is dust, a difficult problem that tar content is high in the pyrolysis coal gas prepared.By adopting high-temperature filter to filter the pyrolysis coal gas containing dust, tar in prior art, the content of the tar in pyrolysis coal gas and dust is significantly reduced, but when life-time service high-temperature filter filters, meeting tar deposits and dust on the filter core of high-temperature filter, blocking filter core, be difficult to remove, reduce the performance of high-temperature filter, affect the removal of tar in pyrolysis coal gas and dust.For another example by adopting the mode of water, ammonia spray washing pyrolysis coal gas, remove the tar in pyrolysis coal gas and dust, but adopt aforesaid way process can produce a large amount of ammoniacal liquor containing tar and dust, again because oil, shipwreck are to be separated, tar in ammoniacal liquor is difficult to recycle, dust is not easy to remove, and produce a large amount of sewage, environmental pollution is serious.Therefore, still there is no now the method better removing the coal-tar middle oil and dust of pyrolysis coal gas.
In prior art, open use contains tar raw gas tar removing, dust device, be generally the washing tower comprising and be provided with raw gas import and raw gas outlet, at least three washing sections are provided with in washing tower, be equipped with washing medium outlet, packing layer and liquid distributor in each washing chill zone from the bottom to top, washing medium outlet is communicated with liquid distributor respectively at storage tank through pump, water cooler.Raw gas enters in washing tower by raw gas import, raw gas flows from the bottom to top to contact with washing section successively and lowers the temperature, successively the dust in raw gas and tar are removed, solve that existing apparatus running cost is high, the problem of complex process and chalk dust removing and tar poor effect.But in such scheme containing tar raw gas tar-removing device also Shortcomings, as in washing raw gas process, raw gas needs the multistage washing through more than at least three washing sections, dust in raw gas and tar could be removed, and also need to be equipped with packing layer in each washing section, such raw gas is increasing through packing layer and the reverse contact heat-exchanging area of washing medium from liquid distributor, so that the dust in raw gas and tar are caught, cause the complex process of raw gas tar removing and dust, refrigerating unit structure is made to become complicated, because the packing layer used in device exists the problem easily by tar and dust blocking, even if the lattice Ritchie grid packing that selectivity is excellent, the problem that packing layer is blocked by tar and dust can not be avoided, after packing layer life-time service, packing layer inner easily accumulation tar and dust result in blockage, therefore after life-time service, packing layer may affect the effect of this device chalk dust removing and tar to a certain extent, filler simultaneously also owing to needing selectivity excellent does packing layer, considerably increase cost, and making due to life-time service packing layer block or damaging, need to change packing layer, dismounting is very inconvenient with maintenance.
Utility model content
For this reason, technical problem to be solved in the utility model is the tripping device complex structure of raw gas dust of the prior art and tar, chalk dust removing and tar poor effect, cost is high, the problems such as inconvenient maintenance, and then provide a kind of chalk dust removing and tar effect is excellent, structure is simple, cost is low and easy to maintenance a kind of raw gas separation system.
For solving the problems of the technologies described above, the utility model provides a kind of separation system of raw gas, comprise tower body, escape pipe is connected with at described tower body top, be provided with raw gas import in described tower body bottom, bottom described tower body, be connected with coke discharging oil pipe, connect the first tar shower on described tower body top, described first tar shower is sealedly connected with the first tar shower nozzle stretching into described tower body inside, described first tar shower nozzle is positioned at the below of the air outlet of described escape pipe; In the middle part of described tower body, connect the second tar shower, described second tar shower is sealedly connected with the second tar shower nozzle stretching into described tower body inside, described second tar shower nozzle is positioned at the below of described first tar shower nozzle; Length between described first tar shower nozzle to described tower body top is the 1/10-2/9 of described tower body total length; Length between described second tar shower nozzle to described tower body top is the 1/2-2/3 of described tower body total length; Length between described raw gas import to described tower body top is the 2/3-4/5 of described tower body total length.
Described separation system, the spray medium of described first tar shower nozzle is tar light oil or tar heavy oil, and the temperature controlling described tar light oil is 35-55 DEG C, and the temperature of tar heavy oil is 80-95 DEG C; The spray medium of described second tar shower nozzle is tar heavy oil, and the temperature controlling described tar heavy oil is 80-95 DEG C.
Described separation system, the specific liquid rate of the spray medium of described first tar shower nozzle is 5-9m
3/ (m
2h), preferred 6-7m
3/ (m
2h); The specific liquid rate of the spray medium of described second tar shower nozzle is 2-7m
3/ (m
2h), preferred 4-5m
3/ (m
2h); Described raw gas is 1-3m/s by the empty tower gas velocity in described tower body 1, preferred 1-2m/s.
Described separation system, the tar temperature bottom described tower body controls as 120-155 DEG C, and the raw gas temperature at described tower body top controls as 85-115 DEG C; Described raw gas controls to be 400 ~ 580 DEG C by the temperature of described raw gas import, and pressure is-0.05KPa-5KPa.
Described separation system, described raw gas import is connected with raw gas inlet pipe, is provided with the push rod that can be free to slide along pipeline in described raw gas inlet pipe, advances pyrolysis of coal inside reactor for the dust will deposited in described raw gas inlet pipe.
Described separation system, described push rod comprises and pushes away ash end and pushing hands end, described in push away ash end and be arranged in described raw gas inlet pipe, described pushing hands end is arranged on described raw gas inlet pipe outside through described raw gas inlet pipe or described tower body.
Described tower body lower side is connected with the second inlet pipe, described second inlet pipe is positioned on the downside of described raw gas inlet pipe, described second inlet pipe is blind end relative to the one end be connected with tower body, the sidewall of described second inlet pipe is provided with described raw gas import, described raw gas inlet pipe is blind end relative to the one end be connected with fire door, described raw gas inlet pipe sidewall is provided with the first inlet pipe, and described first inlet pipe is connected with described raw gas import.
Described pushing hands end, through the blind end of described raw gas inlet pipe, is arranged on the outside of described raw gas inlet pipe.
Preferably, described raw gas inlet pipe is parallel with described second inlet pipe, and described first inlet pipe is parallel with described tower body.
Preferably, described raw gas inlet pipe is vertical with described first inlet pipe.
Described separation system, described coke discharging oil pipe is connected with pump, cooling pool and horizontal screw centrifuge in turn.
Described separation system, the tar in described coke discharging oil pipe is cooled to 80-95 DEG C by described cooling pool.
Described separation system, described escape pipe is connected with oil gas cooling separation and blower fan.Preferably, described blower fan is roots blower or water ring vacuum pump.
Described separation system, the bottom of described tower body inside is provided with agitator.
Described separation system, described raw gas is gas retort pyrolysis coal gas.
When described tar light oil refers to 20 DEG C, density is about 0.95g/cm
3, initial boiling point is about 210 DEG C, and 380 DEG C of quantity of distillate are the coal tar of 60%; When described tar heavy oil refers to 20 DEG C, density is about 1.05g/cm
3 ,initial boiling point is about 75 DEG C, and 300 DEG C of quantity of distillate are the coal tar of 80%.The easily gasification of described tar light oil major part, is convenient to heat to take out of from top, decreases the usage quantity of tar heavy oil, save energy consumption.
Technique scheme of the present utility model has the following advantages compared to existing technology:
(1) separation system of raw gas described in the utility model, comprise tower body, escape pipe is connected with at described tower body top, raw gas import is provided with in described tower body bottom, coke discharging oil pipe is connected with bottom described tower body, connect the first tar shower on described tower body top, described first tar shower is sealedly connected with the first tar shower nozzle stretching into described tower body inside, described first tar shower nozzle is positioned at the below of the air outlet of described escape pipe, in the middle part of described tower body, connect the second tar shower, described second tar shower is connected with the second tar shower nozzle stretching into described tower body inside, described second tar shower nozzle is positioned at the below of described first tar shower nozzle, length between described first tar shower nozzle to described tower body top is the 1/10-2/9 of described tower body total length, length between described second tar shower nozzle to described tower body top is the 1/2-2/3 of described tower body total length, length between described raw gas import to described tower body top is the 2/3-4/5 of described tower body total length, by being provided with the first tar shower nozzle and the second tar shower nozzle on tower body top and middle part, described raw gas enters in tower body through raw gas import, flow from the bottom to top, the tar sprayed out with the second tar shower nozzle and the first tar shower nozzle is successively reverse to be contacted, the tar sprayed out and raw gas carry out heat exchange, the temperature of the raw gas of high temperature is reduced, adsorb the dust in raw gas and tar simultaneously, again due to the first tar shower nozzle, the privileged site that second tar shower nozzle and raw gas import are arranged in described tower body, make the tar processing that described raw gas sprays respectively through the first tar shower nozzle and the second tar shower nozzle, and then the removal of dust in control raw gas and tar, detailed process is that the most of dust carried secretly in raw gas and tar heavy oil wash by the second tar shower nozzle, and the temperature of raw gas obtains and significantly reduces, also reduce the material requirement of equipment, absorb dust in raw gas and burnt oil throwing tar lands at the bottom of tower, then discharged by coke discharging oil pipe, again through the spray of tower top first tar shower nozzle, dust in raw gas is almost by washes clean, also being condensed with tar falls at the bottom of tower, go out that tar light oil in the raw gas of tower is separated in follow-up oil gas cooling separation to get off, achieve the object removing dust in raw gas and tar, described separation system eliminates the use of packing layer, avoid packing layer easily to block, chalk dust removing and tar poor effect after long-term use, need to regularly replace packing layer, cost is high, and the problem of not easy-maintaining, described separation system is due to without the need to using packing layer, structure is made to become simpler, dismounting and easy to maintenance, cost reduces, simultaneously in removal tar in dust and tar effect, the separating effect of described separation system is suitable with the separating effect of the tripping device using packing layer, even higher, solve the tripping device complex structure of raw gas dust of the prior art and tar, chalk dust removing and tar poor effect, cost is high, the problem of inconvenient maintenance.
(2) separation system of raw gas described in the utility model, by being connected with raw gas inlet pipe in described raw gas import, make raw gas before entering tower body inside, dust in raw gas can natural sediment in inlet pipe, reduce the pressure that tower body removes dust in raw gas, then in described raw gas inlet pipe, be provided with the push rod that can be free to slide along pipeline, dust for depositing in described raw gas inlet pipe advances in pyrolysis of coal reactor, avoid dust to block inlet pipe, affect the speed that raw gas enters tower body.
(3) separation system of raw gas described in the utility model, the separation system of raw gas of the present invention, by being connected with the second inlet pipe in described tower body lower side, be located on the downside of described raw gas inlet pipe, described second inlet pipe is blind end relative to the one end be connected with tower body, the sidewall of described second inlet pipe is provided with described raw gas import, described raw gas inlet pipe is relative to being blind end with the one end there be not pyrolysis reactor to be connected, described raw gas inlet pipe sidewall is provided with the first inlet pipe, and described first inlet pipe is connected with described raw gas import, raw gas enter described raw gas inlet pipe then enter via described first inlet pipe be connected with described second inlet pipe tower body in, described raw gas is made to enter the flow direction of tower body inside from the horizontal by certain angle, then in the second inlet pipe, again flow direction is changed, keep parallel with described second inlet pipe, then after entering tower body, again change flow direction from the bottom to top into, in above-mentioned raw gas turning direction process, because the dust weight in raw gas is large, the inertia comparing raw gas is large, dust can not in time and coal gas together change flow direction, dust is different from the direction of motion of raw gas, reach the effect by raw gas and dust separation, depart from the dust of raw gas when lacking power, landing can be deposited on the bottom of the second inlet pipe or the bottom of tower body gradually, dust in inlet pipe is advanced pyrolysis of coal inside reactor by push rod, fall into dust bottom tower body finally along with tar is discharged by coke discharging oil pipe, greatly reduce the content of dust in raw gas.
(4) separation system of raw gas described in the utility model, by described raw gas inlet pipe is parallel with described second inlet pipe, described first inlet pipe is parallel with described tower body, when raw gas enters described first inlet pipe by raw gas inlet pipe, the flow direction of raw gas changes, when entering the second inlet pipe by the first inlet pipe, the flow direction of raw gas changes again, when entering in tower body from the second inlet pipe, raw gas changes again, namely the flow direction of raw gas experienced by the change of three times, and ensure that the angle of transformation is all larger, the flow direction of raw gas is farthest changed in system allowed band, improve the separating effect of raw gas and dust greatly.
(5) separation system of raw gas described in the utility model, described raw gas inlet pipe is vertical with described first inlet pipe, ensure that the degree that each raw gas turns is balanced, avoid flowing in transition process that to there is angle excessive and too small, the easy impact system when angle is excessive, cause system cloud gray model unstable, or damage system, reduce security, when angle too small, turn to the effect removing dust little by raw gas, and it is vertical with described first inlet pipe by described raw gas inlet pipe, the degree that each raw gas is turned is suitable, ensure that the effect that in raw gas, dust is removed, stability and the security of system have been taken into account simultaneously.
(6) separation system of raw gas described in the utility model, by being connected with pump, cooling pool and horizontal screw centrifuge in turn on described coke discharging oil pipe, tar by discharging in coke discharging oil pipe is cooled, then be separated through horizontal screw centrifuge, remove the dust in tar and the dregs of fat, tar after separation can be recycled, as the spray medium in the first tar shower nozzle or the second tar shower nozzle.
(7) separation system of raw gas described in the utility model, by being connected with oil gas cooling separation and blower fan on described escape pipe, by oil and gas separating system, the raw gas removing dust and tar is carried out gas-oil separation, burnt oil and gas in further separation raw gas, then described raw gas intake pressure is passed through by air-blower control raw gas, ensure that coal gas has certain speed and enters tower body inside, be convenient to coal gas and can flow from the bottom to top in tower body inside and contact with spray tar.
(8) separation system of raw gas described in the utility model, be tar heavy oil or tar light oil by controlling the spray medium of described first tar shower nozzle, the temperature controlling described tar heavy oil is 80-95 DEG C, the temperature of described tar light oil is 35-55 DEG C, the spray medium of described second tar shower nozzle is tar heavy oil, the temperature controlling described tar heavy oil is 80-95 DEG C, ensure that raw gas is through different tar processing, dust in absorption raw gas and tar, remove the dust in raw gas and tar greatly, simultaneously owing to carrying out reverse contact heat-exchanging with the tar of low temperature, greatly reduce the temperature of raw gas.
(9) separation system of raw gas described in the utility model is 5-9m by the spray specific liquid rate of the spray medium controlling described first tar shower nozzle
3/ (m
2h); The spray specific liquid rate of the spray medium of described second tar shower nozzle is 2-7m
3/ (m
2h); Described raw gas is 1-3m/s by the empty tower gas velocity in described tower body, significantly increases the contact area of tar and raw gas, and then the dust that improve in absorption raw gas and the efficiency of tar and heat exchange efficiency.
Accompanying drawing explanation
In order to make content of the present utility model be more likely to be clearly understood, below according to specific embodiment of the utility model also by reference to the accompanying drawings, the utility model is described in further detail, wherein
Fig. 1 is the separation system structural representation of the raw gas described in a kind of embodiment of the utility model;
Fig. 2 is the separation system structural representation of the another kind of raw gas described in embodiment of the utility model.
In figure, Reference numeral is expressed as: 1-tower body, 2-escape pipe, the import of 3-raw gas, 4-coke discharging oil pipe, 5-first tar shower, 6-first tar shower nozzle, 7-air outlet, 8-second tar shower, 9-second tar shower nozzle, 10-agitator, 11-pump, 12-cooling pool, 13-horizontal screw centrifuge, 14-oil gas cooling separation, 15-blower fan, 16-raw gas inlet pipe, 17-push rod, 171-pushes away ash end, 172-pushing hands end, 18-first inlet pipe, 19-second inlet pipe.
Embodiment
Be clearly and completely described the technical solution of the utility model below in conjunction with accompanying drawing, obviously, described embodiment is the utility model part embodiment, instead of whole embodiments.Based on the embodiment in the utility model, those of ordinary skill in the art are not making the every other embodiment obtained under creative work prerequisite, all belong to the scope of the utility model protection.
In description of the present utility model, it should be noted that, term " on ", D score, " interior ", the orientation of the instruction such as " outward " or position relationship be based on orientation shown in the drawings or position relationship, only the utility model and simplified characterization for convenience of description, instead of the device of instruction or hint indication or element must have specific orientation, with specific azimuth configuration and operation, therefore can not be interpreted as restriction of the present utility model.In addition, term " first ", " second " only for describing object, and can not be interpreted as instruction or hint relative importance.
In description of the present utility model, it should be noted that, unless otherwise clearly defined and limited, term " connection " should be interpreted broadly, and such as, can be fixedly connected with, also can be removably connect, or connect integratedly; Can be mechanical connection, also can be electrical connection; Can be directly be connected, also indirectly can be connected by intermediary, can be the connection of two element internals.For the ordinary skill in the art, particular case the concrete meaning of above-mentioned term in the utility model can be understood.
In addition, if below in the described different embodiment of the utility model involved technical characteristic do not form conflict each other and just can be combined with each other.
The separation system of a kind of raw gas as shown in Figure 1, comprise tower body 1, escape pipe 2 is connected with at described tower body 1 top, raw gas import 3 is provided with in described tower body 1 bottom, coke discharging oil pipe 4 is connected with bottom described tower body 1, connect the first tar shower 5 on described tower body 1 top, described first tar shower 5 is connected with the first tar shower nozzle 6 stretching into described tower body 1 inside, described first tar shower nozzle 6 is positioned at the below of the air outlet 7 of described escape pipe 2; In the middle part of described tower body 1, connect the second tar shower 8, described second tar shower 8 is connected with the second tar shower nozzle 9 stretching into described tower body 1 inside, described second tar shower nozzle 9 is positioned at the below of described first tar shower nozzle 6; Length between described first tar shower nozzle 6 to described tower body 1 top is the 1/10-2/9 of described tower body 1 total length; Length between described second tar shower nozzle 9 to described tower body 1 top is the 1/2-2/3 of described tower body 1 total length; Length between described raw gas import 3 to described tower body 1 top is the 2/3-4/5 of described tower body total length.
With initial raw gas, (for 400-580 DEG C, tar content is 8% (V) to temperature, and dustiness is 40g/m
3, mass ratio accounts for 12%) enter described tower body 1 inside by described raw gas import 3, then utilize described tower body 1 inside that described first tar shower nozzle 6 is set at specific position, second tar shower nozzle 9 and raw gas import 3, make raw gas enter described tower body 1 inside to flow from the bottom to top, spray medium contact fully with described first tar shower nozzle 6 and the second tar shower nozzle 9, dust in absorption raw gas and tar, eliminate the content of dust in raw gas and tar significantly, raw gas temperature after removal is 85-115 DEG C, after the further separation of oil gas cooling separation 14 and electrically trapped tar oil, tar content is for being less than 1ppm, dustiness is for being less than 3mg/m
3temperature is 40 DEG C, compare and remove dust in raw gas and tar by arranging packing layer in described tower body, avoid packing layer easily to block, chalk dust removing and tar poor effect after long-term use, need to regularly replace packing layer, cost is high, and the problem of not easy-maintaining, described separation system, due to without the need to using packing layer, makes structure become simpler, dismounting and easy to maintenance, cost reduces, and simultaneously in removal tar in dust and tar effect, the separating effect of described separation system is suitable with the separating effect of the tripping device using packing layer.
Further, the spray medium of described first tar shower nozzle 6 is tar heavy oil, and the temperature controlling described tar heavy oil is 80-95 DEG C; The spray medium of described second tar shower nozzle 9 is tar heavy oil, and the temperature controlling described tar heavy oil is 80-95 DEG C.It is inner that raw gas enters described tower body 1 by described raw gas import 3, then under the double spraying effect of the tar heavy oil of described first tar shower nozzle 6 and described second tar shower nozzle 9, reduce the speed that raw gas upwards flows, extend raw gas and described tar heavy oil carries out the reverse contact heat-exchanging time, increase simultaneously and carry out reverse contact heat-exchanging area with described tar heavy oil, the temperature of remarkable reduction raw gas, improve the amount of the coal-tar middle oil and dust of tar heavy oil absorption raw gas simultaneously, the raw gas temperature after purifying is made to be 85-115 DEG C, after the further separation of oil gas cooling separation 14 and electrically trapped tar oil, tar content is for being less than 0.85ppm, dustiness is for being less than 3mg/m
3.
As interchangeable another kind of embodiment, the spray medium of described first tar shower nozzle 6 is tar light oil, and the temperature of described tar light oil is 35-55 DEG C; The spray medium of described second tar shower nozzle 9 is tar heavy oil, and the temperature controlling described tar heavy oil is 80-95 DEG C.By the spray medium of described first tar shower nozzle 6 is replaced with tar light oil, and the temperature controlling tar light oil is 35-55 DEG C, make raw gas after described second tar shower nozzle 9 sprays again through the spray of the first tar shower nozzle 6, reverse contact heat-exchanging is carried out with described tar light oil, the temperature of further reduction raw gas, adsorb the tar light oil in raw gas and dust simultaneously, tar content in further reduction raw gas, the raw gas obtained after purification is temperature 85-115 DEG C, after the further separation of oil gas cooling separation 14 and electrically trapped tar oil, tar content is 0.65ppm, dustiness is for being less than 3mg/m
3.
Further, the specific liquid rate controlling the spray medium of described first tar shower nozzle 6 is 5-9m
3/ (m
2h); The specific liquid rate of the spray medium of described second tar shower nozzle 9 is 2-7m
3/ (m
2h); Described raw gas is 1-3m/s by the empty tower gas velocity in described tower body 1.The empty tower gas velocity in described tower body 1 is passed through by the specific liquid rate and raw gas controlling spray medium, reach the speed reducing raw gas and upwards flow, further prolongation raw gas and tar carry out the reverse contact heat-exchanging time, significantly increase raw gas and described tar carry out reverse contact heat-exchanging area simultaneously, the temperature of remarkable reduction raw gas, and raising tar absorption raw gas is coal-tar middle oil and the amount of dust.The raw gas temperature obtained after purification is 85-115 DEG C, and after the further separation of oil gas cooling separation 14 and electrically trapped tar oil, tar content is for being less than 0.5ppm, and dustiness is for being less than 2mg/m
3.
Further, the specific liquid rate controlling the spray medium of described first tar shower nozzle 6 is 6-7m
3/ (m
2h); The specific liquid rate of the spray medium of described second tar shower nozzle 9 is 4-5m
3/ (m
2h); Described raw gas is 1-2m/s by the empty tower gas velocity in described tower body 1.The raw gas temperature obtained after purification is 85-115 DEG C, and after the further separation of oil gas cooling separation 14 and electrically trapped tar oil, tar content is for being less than 0.4ppm, and dustiness is for being less than 1.5mg/m
3.
Further, the tar temperature bottom described tower body 1 controls as 120-155 DEG C, and the raw gas temperature at described tower body 1 top controls as 85-115 DEG C; Described raw gas controls to be 400 ~ 580 DEG C by the temperature of described raw gas import 3, and pressure is-0.05KPa-5KPa.Be 120-155 DEG C by the tar temperature controlled bottom described tower body 1, prevent dust in the coking of tower bottom sediments, at the bottom of blocking tower, the discharge of unfavorable tar.Being 85-115 DEG C by controlling the raw gas temperature at described tower body 1 top, making described raw gas be convenient to enter in subsequent processing, avoiding too high or too low for temperature, the security of influential system.It is 400 ~ 580 DEG C by controlling described raw gas by the temperature of described raw gas import 3, pressure is-0.05KPa-5KPa, avoid making described raw gas temperature too low, the tar in raw gas is made easily to meet cold junction Jiao when the sidewall of contact system on sidewall, the pipeline of block system, avoid temperature too high simultaneously, the danger coefficient of increase system, improve the security of system cloud gray model, make raw gas have certain pressure simultaneously, object is to ensure that raw gas enters in system with certain speed, ensures the security of system.
Further, described raw gas import 3 is connected with raw gas inlet pipe 16; The push rod 17 that can be free to slide along pipeline is provided with, for the dust of deposition in described raw gas inlet pipe 16 is advanced pyrolysis of coal inside reactor in described raw gas inlet pipe 16.It is concrete that described push rod 17 comprises and pushes away ash end 171 and pushing hands end 172 as shown in Figure 1, described in push away ash end 171 and be arranged in the pipeline of described raw gas inlet pipe 16, it is outside that described pushing hands end 172 is arranged on described tower body 1 through described tower body 1.By connecting described raw gas inlet pipe 16 in described raw gas import 3, dust natural sediment in raw gas is in described raw gas inlet pipe 16, described push rod 17 is set in described raw gas inlet pipe 16 simultaneously, the described ash end 171 that pushes away is arranged in described raw gas inlet pipe 16, described pushing hands end 172 is arranged described tower body 1 through described tower body 1 outside, so that technician is by controlling described pushing hands end 172, push away ash end 171 described in making to slide in described raw gas inlet pipe 16, the dust deposited in pipeline is pushed pyrolysis of coal inside reactor, dust is avoided to block described raw gas inlet pipe 16, affect the flow rate that raw gas enters described tower body 1.The raw gas obtained after purification is temperature is 85-115 DEG C, and after the further separation of oil gas cooling separation 14 and electrically trapped tar oil, tar content is less than 0.4ppm, and dustiness is less than 1.5mg/m
3.
As interchangeable embodiment, as shown in Figure 2, the second inlet pipe 19 is connected with in described tower body 1 lower side, be positioned on the downside of described raw gas inlet pipe 16, described second inlet pipe 19 is blind end relative to the one end be connected with tower body, the top of described second inlet pipe 19 is provided with described raw gas import 3, described raw gas inlet pipe 16 is blind end relative to the one end be connected with pyrolysis of coal reactor, be provided with the first inlet pipe 18 bottom described raw gas inlet pipe 16, described first inlet pipe 18 is connected with described raw gas import 3.Raw gas enters described raw gas inlet pipe 16, then enter via described first inlet pipe 18 in the tower body being connected with described second inlet pipe 19, in the process, after raw gas enters described first inlet pipe 18 from described raw gas inlet pipe 16, the flow direction of described raw gas changes, the weight comparing coal gas due to the dust in raw gas is large, the inertia that dust compares coal gas is large, when raw gas flow direction changes, dust can not in time and coal gas together change flow direction, cause at raw gas when changing, dust is different from the direction of motion of raw gas, raw gas and dust separation, depart from the dust of raw gas when lacking power, landing is deposited on tube wall gradually, when raw gas enters in described second inlet pipe 19 from described first inlet pipe 18, the flow direction of raw gas changes again, flow direction keeps parallel with described second inlet pipe 19, again by raw gas and dust separation, flow direction is changed into flow direction from the bottom to top after raw gas enters described tower body 1 from described second inlet pipe 19, again by raw gas and dust separation, depart from the dust of raw gas when lacking power, landing can be deposited on the bottom of the second inlet pipe or the bottom of tower body gradually, finally along with tar is discharged by coke discharging oil pipe, in above-mentioned raw gas steering procedure, greatly reduce the content of dust in raw gas.The raw gas obtained after purification is temperature is 85-115 DEG C, and after the further separation of oil gas cooling separation 14 and electrically trapped tar oil, tar content is less than 0.4ppm, and dustiness is less than 1mg/m
3.
Further, described pushing hands end 172 is through the blind end of described raw gas inlet pipe 16, be arranged on the outside of described raw gas inlet pipe 16, so that technician is by controlling described pushing hands end 172, push away ash end 171 described in making to slide in described raw gas inlet pipe 16, the dust deposited in pipeline is pushed pyrolysis of coal inside reactor.
Further, described raw gas inlet pipe 16 is parallel with described second inlet pipe 19, and described first inlet pipe 18 is parallel with described tower body 1, so that farthest change the flow direction of raw gas, substantially increases the separating effect of raw gas and dust.
Further, described raw gas inlet pipe 16 is vertical with described first inlet pipe 18, the degree that the flow direction improving raw gas further changes, and significantly improves the separating effect of raw gas and dust.Raw gas is temperature is 85-115 DEG C, after oil gas cooling separation 14 is separated further and electrically trapped tar oil tar content for being less than 0.4ppm, dustiness is for being less than 0.8mg/m
3.
Further, described coke discharging oil pipe 4 is connected with pump 11, cooling pool 12 and horizontal screw centrifuge 13.By arranging described pump 11, to be sucked out by the tar in tower body, avoid tar deposition coking and blocking pipeline bottom described tower body 1.By arranging described cooling pool 12, to reduce the temperature of the tar of discharging, so that the recycling of tar.By arranging described horizontal screw centrifuge 13, for removing dust in tar and the dregs of fat, the tar after separation can recycle, as the spray medium in the second tar shower nozzle, saves cost.
Further, the tar in described coke discharging oil pipe 4 is cooled to 80-95 DEG C by described cooling pool 12, to reduce the temperature of the tar of discharging, to recycle, as the spray medium in the second tar shower nozzle, reaches the effect reduced costs.
Further, described escape pipe 2 is connected with oil gas cooling separation 14 and blower fan 15.By described oil and gas separating system 14, the raw gas removing dust and tar is carried out gas-oil separation, be separated the burnt oil and gas in raw gas further, reduce the tar content in coal gas.Then control raw gas by described raw gas import 3 pressure by described blower fan 15, ensure that coal gas has certain speed and enters described tower body 1 inside, be convenient to coal gas and can flow from the bottom to top in described tower body 1 inside and contact with spray tar.
Further, the bottom of described tower body 1 inside is provided with agitator 10, for preventing tar deposition coking and blocking pipeline bottom described tower body 1.
The present invention by arranging first, second tar spray nozzle at tower body particular position inside, and is tar light oil or tar heavy oil by the spray medium of control first tar spray nozzle, because when spray medium is 20 DEG C, density is 0.95g/cm
3tar light oil, or when 20 DEG C, density is about 1.05g/cm
3tar heavy oil, significantly can adsorb the dust in raw gas and tar, when being 20 DEG C by controlling the spray medium of the second tar spray nozzle, density is about 1.05g/cm
3tar heavy oil, this tar heavy oil significantly can adsorb dust in raw gas and tar, and greatly reduce the content of tar in raw gas and dust, be 8% (V) by the tar content in initial raw gas, dust content is 40mg/m
3, mass ratio accounts for 12%, and be significantly reduced to by the raw gas tar content obtained after above-mentioned steps purification and be less than 1ppm, dust content is significantly reduced to 3mg/m
3below, significant technique effect is obtained.
Obviously, above-described embodiment is only for clearly example being described, and the restriction not to embodiment.For those of ordinary skill in the field, can also make other changes in different forms on the basis of the above description.Here exhaustive without the need to also giving all embodiments.And thus the apparent change of extending out or variation be still among the protection domain of the invention.
Claims (10)
1. the separation system of a raw gas, comprise tower body (1), escape pipe (2) is connected with at described tower body (1) top, raw gas import (3) is provided with in described tower body (1) bottom, coke discharging oil pipe (4) is connected with in described tower body (1) bottom, it is characterized in that, the first tar shower (5) is connected on described tower body (1) top, described first tar shower (5) is connected with and stretches into the first inner tar shower nozzle (6) of described tower body (1), described first tar shower nozzle (6) is positioned at the below of the inlet mouth (7) of described escape pipe (2), the second tar shower (8) is connected at described tower body (1) middle part, described second tar shower (8) is connected with and stretches into the second inner tar shower nozzle (9) of described tower body (1), described second tar shower nozzle (9) is positioned at the below of described first tar shower nozzle (6), length between described first tar shower nozzle (6) to described tower body (1) top is the 1/10-2/9 of described tower body (1) total length, length between described second tar shower nozzle (9) to described tower body (1) top is the 1/2-2/3 of described tower body (1) total length, length between described raw gas import (3) to described tower body (1) top is the 2/3-4/5 of described tower body total length.
2. separation system according to claim 1, is characterized in that, described raw gas import (3) is connected with raw gas inlet pipe (16); The push rod (17) that can be free to slide along pipeline is provided with, for the dust of deposition in described raw gas inlet pipe (16) is advanced pyrolysis of coal inside reactor in described raw gas inlet pipe (16).
3. separation system according to claim 2, it is characterized in that, described push rod (17) comprise push away ash end (171) and pushing hands end (172), described ash end (171) that pushes away is arranged in the pipeline of described raw gas inlet pipe (16), and described pushing hands end (172) is arranged on described raw gas inlet pipe (16) outside or described tower body (1) outside through described raw gas inlet pipe (16) or described tower body (1).
4. the separation system according to any one of claim 1-3, it is characterized in that, described tower body (1) lower side is connected with the second inlet pipe (19), described second inlet pipe (19) is positioned at described raw gas inlet pipe (16) downside, described second inlet pipe (19) is blind end relative to the one end be connected with described tower body (1), the sidewall of described second inlet pipe (19) is provided with described raw gas import (3), described raw gas inlet pipe (16) is blind end relative to the one end be connected with pyrolysis of coal reactor, described raw gas inlet pipe (16) sidewall is provided with the first inlet pipe (18), described first inlet pipe (18) is connected with described raw gas import (3).
5. separation system according to claim 4, is characterized in that, described raw gas inlet pipe (16) is parallel with described second inlet pipe (19), and described first inlet pipe (18) is parallel with described tower body (1).
6. separation system according to claim 4, is characterized in that, described raw gas inlet pipe (16) is vertical with described first inlet pipe (18).
7. the separation system according to any one of claim 1-3 or 5 or 6, is characterized in that, described coke discharging oil pipe (4) is connected with pump (11), cooling pool (12) and horizontal screw centrifuge (13); Described escape pipe (2) is connected with oil gas cooling separation (14) and blower fan (15).
8. separation system according to claim 7, is characterized in that, the spray medium of described first tar shower nozzle (6) is tar heavy oil or tar light oil, and the temperature controlling described tar heavy oil is 80-95 DEG C, and the temperature of described tar light oil is 35-55 DEG C; The spray medium of described second tar shower nozzle (9) is tar heavy oil, and the temperature controlling described tar heavy oil is 80-95 DEG C.
9. the separation system according to any one of claim 1-3 or 5 or 6 or 8, is characterized in that, the specific liquid rate of the spray medium of described first tar shower nozzle (6) is 5-9m
3/ (m
2h); The specific liquid rate of the spray medium of described second tar shower nozzle (9) is 2-7m
3/ (m
2h); Described raw gas is 1-3m/s by the empty tower gas velocity in described tower body (1).
10. separation system according to claim 9, is characterized in that, the tar temperature of described tower body (1) bottom controls as 120-155 DEG C, and the raw gas temperature at described tower body (1) top controls as 85-115 DEG C; Described raw gas controls to be 400 ~ 580 DEG C by the temperature of described raw gas import (3), and pressure is-0.05KPa-5KPa.
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| CN201520732098.XU CN205024184U (en) | 2015-09-21 | 2015-09-21 | Piece -rate system of raw gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105713630A (en) * | 2016-03-31 | 2016-06-29 | 陕西煤业化工集团神木天元化工有限公司 | Coal carbonization, oil-gas washing separation and delayed coking combined technology and device |
| CN110090510A (en) * | 2018-01-29 | 2019-08-06 | 神华集团有限责任公司 | Gu de- be fixedly mounted with of oil gas sets and its applies, consolidates oil gas de-solid method |
-
2015
- 2015-09-21 CN CN201520732098.XU patent/CN205024184U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105713630A (en) * | 2016-03-31 | 2016-06-29 | 陕西煤业化工集团神木天元化工有限公司 | Coal carbonization, oil-gas washing separation and delayed coking combined technology and device |
| CN110090510A (en) * | 2018-01-29 | 2019-08-06 | 神华集团有限责任公司 | Gu de- be fixedly mounted with of oil gas sets and its applies, consolidates oil gas de-solid method |
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