CN102861450A - Reduced-pressure short-path distilling device and spontaneous combustion decoking method of heater of reduced-pressure short-path distilling device - Google Patents
Reduced-pressure short-path distilling device and spontaneous combustion decoking method of heater of reduced-pressure short-path distilling device Download PDFInfo
- Publication number
- CN102861450A CN102861450A CN2012103230010A CN201210323001A CN102861450A CN 102861450 A CN102861450 A CN 102861450A CN 2012103230010 A CN2012103230010 A CN 2012103230010A CN 201210323001 A CN201210323001 A CN 201210323001A CN 102861450 A CN102861450 A CN 102861450A
- Authority
- CN
- China
- Prior art keywords
- feed liquid
- heat
- passage
- heater
- heated
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 32
- 238000002485 combustion reaction Methods 0.000 title claims abstract description 25
- 230000002269 spontaneous effect Effects 0.000 title claims abstract description 22
- 238000005235 decoking Methods 0.000 title abstract 3
- 239000007788 liquid Substances 0.000 claims abstract description 303
- 238000001704 evaporation Methods 0.000 claims abstract description 62
- 238000004939 coking Methods 0.000 claims abstract description 48
- 239000000463 material Substances 0.000 claims abstract description 48
- 230000008020 evaporation Effects 0.000 claims abstract description 42
- 238000004821 distillation Methods 0.000 claims abstract description 28
- 238000010438 heat treatment Methods 0.000 claims abstract description 25
- 230000006837 decompression Effects 0.000 claims description 25
- 238000004140 cleaning Methods 0.000 claims description 19
- 239000000571 coke Substances 0.000 claims description 17
- 238000010521 absorption reaction Methods 0.000 claims description 15
- 230000008676 import Effects 0.000 claims description 12
- 241000628997 Flos Species 0.000 claims description 10
- 230000033228 biological regulation Effects 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 6
- 230000007246 mechanism Effects 0.000 claims description 6
- 238000004891 communication Methods 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 5
- 230000000630 rising effect Effects 0.000 claims description 4
- 239000007791 liquid phase Substances 0.000 claims description 3
- 230000002441 reversible effect Effects 0.000 claims description 3
- 241000439496 Varanus dumerilii Species 0.000 claims description 2
- 230000002045 lasting effect Effects 0.000 claims description 2
- 238000000197 pyrolysis Methods 0.000 abstract description 6
- 230000015572 biosynthetic process Effects 0.000 abstract description 5
- 230000001052 transient effect Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 10
- 230000000694 effects Effects 0.000 description 6
- 231100000331 toxic Toxicity 0.000 description 6
- 230000002588 toxic effect Effects 0.000 description 6
- 230000008901 benefit Effects 0.000 description 5
- 239000012071 phase Substances 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 238000009835 boiling Methods 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000012535 impurity Substances 0.000 description 3
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 238000005292 vacuum distillation Methods 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- 230000008016 vaporization Effects 0.000 description 3
- 239000002912 waste gas Substances 0.000 description 3
- 235000002918 Fraxinus excelsior Nutrition 0.000 description 2
- 239000002956 ash Substances 0.000 description 2
- 230000002950 deficient Effects 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 239000011368 organic material Substances 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 230000004888 barrier function Effects 0.000 description 1
- 239000003818 cinder Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000001771 impaired effect Effects 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 230000000505 pernicious effect Effects 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 238000002207 thermal evaporation Methods 0.000 description 1
- 230000008646 thermal stress Effects 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a distilling device, in particular to a reduced-pressure short-path distilling device and a spontaneous combustion decoking method of a heater of the reduced-pressure short-path distilling device. According to the reduced-pressure short-path distilling device, the heater is a double-channel heat exchanger arranged outside an evaporator, one channel of the double-channel heat exchanger is a feed liquid heating channel, a feed liquid heating channel entrance is communicated with a feed liquid discharge outlet of the evaporator by a heated feed liquid input pipeline and a feed liquid delivery pump, and a feed liquid heating channel exit is communicated with a high position feed liquid evaporating channel entrance of the evaporator by a heated feed liquid output pipeline. The other channel of the double-channel heat exchanger is a heat carrier heat releasing channel, and a heat carrier heat releasing channel entrance and a heat carrier heat releasing channel exit are communicated with a heat carrier circulation pipeline. By utilizing the reduced-pressure short-path distilling device and the spontaneous combustion decoking method, selective and sequential transient heating is provided for feed liquid with reduced pressure distillation to realize efficient evaporation by utilizing the double-channel heat exchanger, the degree of pyrolysis of distilled feed liquid is efficiently restrained, formation of coking materials in the evaporator can be also restrained, and harmless efficient removal of the coking materials of a heating releasing face can be realized through spontaneous combustion.
Description
Technical field
The present invention relates to for example distilling apparatus of waste lubricating oil of organic materials, particularly a kind of spontaneous combustion coke cleaning method of reduce pressure short course distillation device and heater thereof.
Background technology
Decompression distillation is a kind of distillating method of realizing reducing the energy-conservation of feed liquid boiling temperature and suppressing to distill the feed liquid pyrolysis by reducing air pressure, be widely used at present, but the degree and the coking material in inhibition heater coking and the removing heater that suppress the pyrolysis of distillation feed liquid are the focuses that current order distillation those skilled in the art pay close attention to.
Tradition decompression distillation device as shown in Figure 4, its operation principle is:
With feed liquid by pan feeding valve 22 and pan feeding pipeline 21 notes in evaporimeter 20, its injection rate accounts for about 1/2nd of evaporimeter 20 volumes, thus at evaporimeter 20 interior formation low level feed liquid liquid levels 24.
Open feed liquid delivery pump 32, the heat absorption coil pipe that makes the feed liquid of low level feed liquid liquid level below 24 pass through tube furnace via feed liquid floss hole 30, the feed liquid of being heated intake pipeline 31 enters in the high-order feed liquid evaporation channel 14 via the feed liquid export pipeline 12 that is heated, form high-order feed liquid evaporating surface 15 in the exit of high-order feed liquid evaporation channel 14, this liquid level is constantly carried under the prerequisite of feed liquid at feed liquid delivery pump 32, the feed liquid of high-order feed liquid evaporating surface below 15 constantly updated, and feed liquid constantly from inside to outside, trickling is disposed under the low level feed liquid liquid level 24 of evaporimeter 20 inside from top to bottom.
Light the fuel within the tube furnace burning heat release chamber, the feed liquid of circular flow is carried out heat release in the heat absorption coil pipe.
Feed temperature after being heated constantly rises, when reaching the evaporating temperature of feed liquid under its vacuum pressure, Evaporation Phenomenon begins to occur, this moment is in high-order feed liquid evaporating surface 15, constantly having the high temperature gas phase distillate that is vaporized to break away from high-order feed liquid evaporating surface 15 constantly rises and enters in the condenser 18 via distillate exhaust outlet 16, distillate gathering line 17, the feed liquid that can not be vaporized evaporation will be from inside to outside, trickling is disposed under the low level feed liquid liquid level 24 of evaporimeter 20 inside from top to bottom, continues to accept that circulation is heated, circulating and evaporating.
Enter the high temperature gas phase distillate of condenser 18 under the effect of cooling, be liquefied as distillate 26 and enter in the distillate collecting tank 27 via distillate gathering line 17, the waste gas of the liquefaction that can not be cooled is discharged into the external world via toxic emission pipeline 23 and vavuum pump 19.
Under the operating mode of continuous vaporization, impurity and residue content in the feed liquid will improve constantly, and when reaching the expection standard, raffinate is discharged into the external world via residual liquid discharge mouth 28, residual liquid discharge valve 29.
The defective that decompression distillation device shown in Figure 4 exists is:
Be that vacuum distillation apparatus is made heater 1 with tube furnace, although can make feed liquid realize the advantages such as the instantaneous preferential evaporation that is heated, suppress to be distilled the degree of pyrolysis of feed liquid with this, but work as the heat absorption coil pipe of tube furnace within it under reduced pressure under the operating mode of the feed liquid heat release of flowing, be very easy to make heat absorption coil pipe inside to form hard coking material because heat release causes the feed liquid evaporation, in case within the heat absorption coil pipe, form hard coking material, so with regard to present prior art, can only could solve this technical barrier by the heat absorption coil pipe that more renews, if fail in time to find in case within the heat absorption coil pipe, form hard coking material, be very easy to so descend because coking causes the heat transfer property of heat absorption coil pipe, the coil pipe that will absorb heat at short notice burns and causes pernicious security incident.
Another traditional decompression distillation device as shown in Figure 5, its operation principle is:
With feed liquid by pan feeding valve 22 and pan feeding pipeline 21 notes in evaporimeter 20, its injection rate accounts for about 1/2nd of evaporimeter 20 volumes, thus at evaporimeter 20 interior formation low level feed liquid liquid levels 24.
Open feed liquid delivery pump 32, the feed liquid of low level feed liquid liquid level below 24 entered in the high-order feed liquid evaporation channel 14 via feed liquid floss hole 30, the feed liquid of being heated intake pipeline 31, form high-order feed liquid evaporating surface 15 in the exit of high-order feed liquid evaporation channel 14, this liquid level is constantly carried under the prerequisite of feed liquid at feed liquid delivery pump 32, the feed liquid of high-order feed liquid evaporating surface below 15 constantly updated, and feed liquid constantly from inside to outside, trickling is disposed under the low level feed liquid liquid level 24 of evaporimeter 20 inside from top to bottom.
Utilize high-temperature heat carrier in the heat release coil pipe, to circulate, for the feed liquid of evaporimeter 20 interior low level feed liquid liquid levels below 24 carried out heat release.
Feed temperature after being heated constantly rises, when reaching the evaporating temperature of feed liquid under its vacuum pressure, Evaporation Phenomenon begins to occur, this moment is in the feed liquid liquid level, constantly having the high temperature gas phase distillate that is vaporized to break away from the feed liquid liquid level constantly rises and enters in the condenser 18 via distillate exhaust outlet 16, distillate gathering line 17, the feed liquid that can not be vaporized evaporation in high-order feed liquid evaporation channel 14 will be from inside to outside, trickling is disposed under the low level feed liquid liquid level 24 of evaporimeter 20 inside from top to bottom, continues to accept that circulation is heated, circulating and evaporating.
Enter the high temperature gas phase distillate of condenser 18 under the effect of cooling, be liquefied as distillate 26 and enter in the distillate collecting tank 27 via distillate gathering line 17, the waste gas of the liquefaction that can not be cooled is discharged into the external world via toxic emission pipeline 23 and vavuum pump 19.
Under the operating mode of continuous vaporization, impurity and residue content in the feed liquid will improve constantly, and when reaching the expection standard, raffinate is discharged into the external world via residual liquid discharge mouth 28, residual liquid discharge valve 29.
The defective of this decompression distillation device existence is as shown in Figure 5:
Be that vacuum distillation apparatus is made heater 1 with the heat release coil pipe, although can be by the artificial coking material of removing outside the heat release coil pipe in evaporimeter 20, but the structure that is based on this device limits, feed liquid can not be carried out an amount of, sequential heating and realize preferential evaporation, finally cause the degree of pyrolysis that is distilled feed liquid high, heat energy consumption height, inefficiency.
Summary of the invention
The object of the invention is to overcome the deficiency of background technology, and provide a kind of selective, have succession ground to realize decompression distillation and can realize the decompression short course distillation device of heater scarfing cinder and the spontaneous combustion coke cleaning method of heater thereof by the coking material spontaneous combustion for the instantaneous heating of feed liquid.
The present invention solves its technical problem and adopts following technical scheme:
A kind of decompression short course distillation device, comprise evaporimeter, feeding mechanism, feed liquid heating arrangements, the distillate cooling collection mechanism of decompressor, heater in the described feed liquid heating arrangements is the double passage heat exchanger that is arranged at outside the evaporimeter, a passage in this double passage heat exchanger is the feed liquid heated passage, its feed liquid heated passage entrance is communicated with the feed liquid floss hole of evaporimeter by be heated feed liquid intake pipeline and feed liquid delivery pump, and its feed liquid heated passage outlet is communicated with the high-order feed liquid evaporation channel entrance of evaporimeter by the feed liquid export pipeline that is heated; Another passage in this double passage heat exchanger is heat carrier heat release passage, and its import and export is communicated with the heat carrier pipeloop.
Adopt the present invention of technique scheme compared with prior art, its outstanding effect is: utilize the Dual-channel type heat exchanger to realize high-efficiency evaporating for the feed liquid of decompression distillation provides selectively, has the instantaneous heating of succession, not only can efficiently suppress to be distilled the degree of pyrolysis of feed liquid, also can suppress the formation of coking material in the evaporimeter, heat delivery surface can also be realized that by self-burning innoxious high-efficient cleaning removes because of the coking material that heat release causes the feed liquid evaporation to form.
As preferably, the present invention further technical scheme is:
Described double passage heat exchanger is a binary channels tubular heat exchanger.
Be provided with FlexbleJoint on the outer cylinder body of described binary channels tubular heat exchanger.
On the feed liquid intake pipeline that is heated between the feed liquid heated passage entrance of described heater and the feed liquid delivery pump check valve is installed.
On the feed liquid export pipeline that is heated between the feed liquid heated passage outlet of described heater and the high-order feed liquid evaporation channel entrance of evaporimeter barostat is installed.
A kind of spontaneous combustion coke cleaning method of heater of the short course distillation device that reduces pressure, carry out as follows:
A. with the discharging of the feed liquid in the feed liquid heated passage of heater totally, and with feed liquid heated passage entrance and the outlet of feed liquid heated passage be in communication with the outside;
B. pass into more than 100 ℃ the heat carrier heat release of flowing in the heat carrier heat release passage, and more than the temperature to 200 of incremental rising heat carrier ℃, make that the liquid phase component among the coking material is evaporated release in the feed liquid heated passage, when evaporation release is complete, the temperature of coking material will constantly rise, by spontaneous combustion or light and make it enter burning heat release state;
C. continue in heat carrier heat release passage, to pass into heat carrier, flow by the lasting of heat carrier, with coking material in the feed liquid heated passage because of the absorption of flowing of the heat that discharges of burning, make the heater of this moment be in reverse heat absorption state, the heat carrier of this moment not only no longer needs extraneous heating combined equipment for its heating, can also carry out suitable heat release with hot equipment to other;
D. monitor heat carrier exhaust temperature and the thermal current exhaust temperature of the outlet of heat carrier heat release channel outlet and feed liquid heated passage, understand the heat release degree of its self-burning, the air demand of control feed liquid heated passage porch, the heat that coking material is discharged in spontaneous combustion process further are controlled in the combustion reference temperature that heater can bear.
The present invention who adopts technique scheme with compare with traditional processing method, have the following advantages:
1. make its mode that turns to dust and ashes by the state with coking material self-burning in the heater, and realize its high-efficient cleaning is removed.
2. for not damage of device, technique is simple, and energy consumption is low.
As preferably, the present invention further technical scheme is:
The method of control air demand is in the described steps d: in order dieseling to be maintained slowly and don't the relative low temperature heat release state that extinguishes, gas supply regulation is originally stated the minimum state that needs to keeping.
The method of control air demand is in the described steps d: be discharged into the external world for the heat that dieseling is discharged carries it with relative maximization air-flow, gas supply regulation is originally stated the maximum rating that needs to keeping, be equipped with air blast at feed liquid heated passage entrance.
Described feed liquid heated passage outlet is equipped with the thermal current conveyance conduit that connects boiler furnace and discharge thermal current to boiler furnace.
The method of lighting coking material among the described step b is: with blowtorch flame is sprayed on the coking material in the feed liquid heated passage by feed liquid heated passage entrance.
Of particular note:
1. heat carrier can use the materials such as conduction oil or fused salt.
2. different by its ignition temperature of different medium coking material that feed liquid forms, also different for the performance of withstand high temperatures by the heater that different materials consists of, so far the temperature in the spontaneous combustion coke cleaning method of above-mentioned heater can't quantize with concrete numeral.
3. because of structure and the different sizes of heater, so far the air demand in the spontaneous combustion coke cleaning method of above-mentioned heater can't quantize with concrete numeral.
4. this heater spontaneous combustion coke cleaning technique is not only limited to for the supporting heater of said apparatus, also can
Be used for the heater that other is fit to this technique coke cleaning, everyly this technique is used for the heater coke cleaning that this technique limits all belongs within technical scheme of the present invention.
Description of drawings
Fig. 1 is the structural representation of vacuum distillation apparatus of the present invention.
Fig. 2 is the section structure schematic diagram of heater of the present invention.
Fig. 3 is the spontaneous combustion coke cleaning view of heater of the present invention.
Fig. 4 is a kind of traditional decompression distillation device structural representation.
Fig. 5 is another kind of traditional decompression distillation device structural representation.
The specific embodiment
Further set forth the present invention below by embodiment and accompanying drawing, purpose only is to understand better content of the present invention.
Referring to Fig. 1, Fig. 2, Fig. 3 is among the figure: heater 1, FlexbleJoint 2, heat exchange core pipe 3, tube sheet 4, heat carrier heat release channel outlet 5, feed liquid heated passage outlet 6, heat carrier heat release passage 7, feed liquid heated passage 8, heat carrier heat release feeder connection 9, heater support 10, feed liquid heated passage entrance 11, the feed liquid of being heated export pipeline 12, barostat 13, high-order feed liquid evaporation channel 14, high-order feed liquid evaporating surface 15, distillate exhaust outlet 16, distillate gathering line 17, condenser 18, vavuum pump 19, evaporimeter 20, feed liquid intake pipeline 21, feed liquid input valve 22, toxic emission pipeline 23, low level feed liquid liquid level 24, evaporator support 25, distillate 26, distillate collecting tank 27, residual liquid discharge mouth 28, residual liquid discharge valve 29, feed liquid floss hole 30, the feed liquid of being heated intake pipeline 31, feed liquid delivery pump 32, check valve 33.
In the present embodiment, evaporimeter 20 is vertical tank containers, be placed on the evaporator support 25, be provided with distillate exhaust outlet 16 at its top, end at its sidepiece is provided with the downward feed liquid intake pipeline 21 of outlet, the other end at its sidepiece is provided with the high-order feed liquid evaporation channel 14 that is formed by reducing tubulose body cavity body, is respectively arranged with residual liquid discharge mouth 28 and feed liquid floss hole 30 in its bottom, and liquid vent valves 29 is connected with the port of export of residual liquid discharge mouth 28.
High-order feed liquid evaporation channel 14 in the present embodiment is to be formed by the cavity of reducing tubular body, the osculum end of this reducing tubular body is import, be arranged at the outside of evaporimeter 20, the big opening end of this reducing tubular body is outlet, is arranged at the inner and upper central authorities of the evaporimeter 20 under the distillate exhaust outlet 16.
The basic function of high-order feed liquid evaporation channel 14 is that it can form high-order feed liquid evaporating surface 15 between low level feed liquid liquid level 24 and feed liquid heated passage outlet 6, high-order feed liquid evaporation channel 14 not only is confined to said structure thus, and it also can finish above-mentioned basic function by other structure.
Feed liquid intake pipeline 21 and feed liquid input valve 22 form feeding mechanism, and feed liquid intake pipeline 21 passes through evaporimeter 20 sidewalls, and the port of export that is downward floss hole is arranged at the inside of evaporimeter 20, and the entrance point of feed liquid intake pipeline 21 is connected with feed liquid input valve 22.
The feed liquid heating arrangements mainly is comprised of the feed liquid intake pipeline 31 that is heated, feed liquid delivery pump 32, heater 1, the feed liquid of being heated export pipeline 12.
The import of the feed liquid of being heated intake pipeline 31 is communicated with feed liquid floss hole 30, the outlet of the feed liquid of being heated intake pipeline 31 is communicated with the feed liquid heated passage entrance 11 of heater 1, between the import of the feed liquid intake pipeline 31 that is heated and outlet, be provided with feed liquid delivery pump 32, the entrance point of the feed liquid of being heated export pipeline 12 is communicated with the feed liquid heated passage of heater 1 outlet 6, the port of export of the feed liquid of being heated export pipeline 12 is communicated with the import of high-order feed liquid evaporation channel 14, the circulation that forms the thus feed liquid route that is heated.
The distillate cooling is collected the mechanism of decompressor mainly by distillate gathering line 17, condenser 18, distillate collecting tank 27, toxic emission pipeline 23 and vavuum pump 19 form, one end of distillate gathering line 17 is communicated with distillate exhaust outlet 16, the other end passes through condenser 18 and is communicated with the import of distillate collecting tank 27, distillate collecting tank 27 is that a vertical tank container is placed on the support, its upper end is provided with import and the outlet of inserting appropriate depth, its internal gathering has distillate 26, and the import of vavuum pump 19 is communicated with by the outlet of toxic emission pipeline 23 with distillate collecting tank 27.
The import of the feed liquid of being heated intake pipeline 31 is communicated with the feed liquid floss hole of feed liquid storage tank via the feed valve, the outlet of the feed liquid of being heated intake pipeline 31 is communicated with the feed liquid heated passage entrance 11 of heater 1, between the import of the feed liquid intake pipeline 31 that is heated and outlet, be provided with feed liquid delivery pump 32, the entrance point of the feed liquid of being heated export pipeline 12 is communicated with the feed liquid heated passage of heater 1 outlet 6, the port of export of the feed liquid of being heated export pipeline 12 is communicated with the import of high-order feed liquid evaporation channel 14, feed liquid floss hole 30 is carried out shutoff closes, residual liquid discharge valve 29 is communicated with the raffinate collecting tank, and what can form thus feed liquid once is subjected to the thermal evaporation route.
When the feed liquid heated passage 8 internal cause heat releases of heater 1 cause the feed liquid evaporation and when forming coking material and when needing to remove, feed liquid heated passage entrance 11 and feed liquid heated passage outlet 6 need to be in communication with the outside.
As preferred version, double passage heat exchanger in the present embodiment is one and places the binary channels tubular heat exchanger outside the evaporimeter 20, it is by outer cylinder body, heat exchange core pipe 3, tube sheet 4, heat carrier heat release channel outlet 5, feed liquid heated passage outlet 6, heat carrier heat release passage 7, feed liquid heated passage 8, heat carrier heat release feeder connection 9, heater support 10, feed liquid heated passage entrance 11 forms, outer cylinder body is a vertical structure tank container, be installed on the heater support 10, the two ends of inner barrel are welded with respectively two tube sheets 4 outside, some radiator body core pipes 3 be angle arranged side by side pass through two tube sheets 4 and with its welding, inner barrel forms two autonomous channels outside thus, the heat carrier heat release passage 7 that had both been consisted of by core pipe inside and the feed liquid heated passage 8 that is consisted of by core pipe outside, below the heat carrier heat release passage 7 and above be communicated with respectively heat carrier heat release feeder connection 9 and the heat carrier heat release channel outlet 5 that is communicated with heating, below the feed liquid heated passage 8 and above be communicated with respectively feed liquid heated passage entrance 11 and feed liquid heated passage and export 6.
The above-mentioned binary channels tubular heat exchanger that places outside the evaporimeter 20 can make heater 1 have under the prerequisite of larger heat exchange area in less space, and the simplification of implement device structure.
Be provided with FlexbleJoint 2 on the outer cylinder body of the tubular heat exchanger of binary channels described in the present embodiment.But the thermal stress between FlexbleJoint 2 efficient absorption heat exchange core pipes 3 and the outer cylinder body.
Among the feed liquid intake pipeline 31 between the delivery pump of feed liquid described in the present embodiment 32 and the feed liquid heated passage entrance 11 check valve 33 is installed.Can make feed liquid heated passage 8 interior holding for a long time that feed liquid is arranged, the feed liquid passage internal cause that the static pressure that produces by feed liquid suppresses heater 1 is heated and is caused the feed liquid evaporation to form coking material.
Among the feed liquid export pipeline 12 that is heated between the heated passage of feed liquid described in present embodiment entrance 11 and the high-order feed liquid evaporation channel 14 barostat 13 is installed.Can make and hold the feed liquid that has in the feed liquid heated passage 8 in the work and be under the positive pressure environment, realize suppressing the feed liquid evaporation by changing the air pressure environment, by suppressing the feed liquid evaporation, realize suppressing the generation of coking material in the feed liquid passage.
The operation principle of present embodiment decompression short course distillation device is summarized as follows:
With feed liquid by pan feeding valve 22 and pan feeding pipeline 21 notes in evaporimeter 20, its injection rate accounts for about 1/2nd of evaporimeter 20 volumes.
Open feed liquid delivery pump 32, the feed liquid in the evaporimeter 20 is heated being heated to circulate in the route with heater 1 diconnected circulation, realize back and forth evaporation.
Feed liquid is under the operating mode that constantly circulation is heated, its temperature constantly rises, when the evaporating temperature that reaches under its vacuum pressure, Evaporation Phenomenon begins to occur, form high-order feed liquid evaporating surface 15 in high-order feed liquid evaporation channel 14 exits this moment, the feed liquid that flow to evaporimeter 20 inner chambers below after evaporation has formed again low level feed liquid liquid level 24, at this moment in the high-order feed liquid evaporating surface 15 under the distillate exhaust outlet 16 in evaporimeter 20, constantly there is the high temperature gas phase distillate that is vaporized to break away from that high-order feed liquid evaporating surface 15 constantly rises and via distillate exhaust outlet 16, distillate gathering line 17 enters in the condenser 18, under the effect of cooling, be liquefied as distillate 26 and enter in the distillate collecting tank 27 via distillate gathering line 17, the waste gas of the liquefaction that can not be cooled is discharged into the external world via toxic emission pipeline 23 and vavuum pump 19.
In the process of continual evaporation, in order to keep the expection liquid level scope of evaporimeter 20 interior feed liquids, can be with new feed liquid via in feed liquid input valve 22, the feed liquid intake pipeline 21 slow feed liquids that at the uniform velocity are injected in the evaporimeter 20.
Under the operating mode of continuous vaporization, impurity and residue content in the feed liquid will improve constantly, and when reaching the expection plan, raffinate is discharged in the raffinate collecting tank via residual liquid discharge mouth 28, residual liquid discharge valve 29.
In the present invention, high-order feed liquid evaporating surface 15 is relative coexistences with low level feed liquid liquid level 24, high-order feed liquid evaporating surface 15 is to deliver to the feed liquid liquid level that evaporates under the distillate exhaust outlet 16 by the feed liquid delivery pump 32 rear feed liquid of will being heated, and the feed liquid liquid level that flow to its below after evaporation is low level feed liquid liquid level 24.
Be heated when feed liquid heated passage 8 internal causes of heater 1 and cause feed liquid evaporation and form coking material and when needing to remove, need all to discharge the feed liquid in this passage clean, feed liquid heated passage entrance 11 and the feed liquid heated passage outlet 6 of this passage are in communication with the outside, inflammable articles are on every side moved to the safety area in a distant place, by heat carrier mobile heat release in heat carrier heat release passage, and constantly carry out incremental intensification and regulate, the feed liquid that this moment, coking material included is discharged by preferential evaporation under the operating mode of heat carrier heat release, until be evaporated when discharging oil gas or smog and being reduced to a certain degree, the heat carrier temperature can rise at a slow speed gradually.
When feed liquid heated passage 8 interior formation coking material, most coking materials are attached on the heating surface of feed liquid heated passage 8, and the heat carrier of this moment is the thermal source of heat carrier heat release passage 7 heat delivery surfaces, forms heat-transfer surface thus between heating surface and heat delivery surface.
There is respectively high-temperature heat carrier and the coking material of organic materials and an amount of oxygen of continuous circulation heat release on the two sides of heat-transfer surface, under this operating mode, the feed liquid that coking material includes at high temperature preferentially is evaporated release, after the evaporation release phenomenon stops, the temperature of coking material will constantly rise to it more than ignition temperature under the operating mode of heat carrier heat release, both can make by the temperature that surmounts self-ignition point coking material enter self-burning heat release state this moment
Can also coking material be lighted by human factor makes coking material enter self-burning heat release state, appearance exothermic phenomenon with the self-burning phenomenon also manifests simultaneously, under the effect of self-burning heat release, the feed liquid heated passage 8 interior thermal currents that will produce a large amount of continuous risings, this thermal current is discharged into the external world via feed liquid heated passage outlet 6, therefore certainly lead to negative pressure at feed liquid heated passage entrance 11 places, outside air or oxygen are under the effect of negative pressure, enter in the feed liquid heated passage 8 via feed liquid heated passage entrance 11, just for the self-burning phenomenon provides oxygen, be thus the condition that provides sufficient of continuing of self-burning phenomenon.
Under the interior operating mode continuing the self-burning heat release of feed liquid passage, although coking material can be turned to dust and ashes, but its temperature is in continuous rising, for fear of each parts of heater 1 at its high temperature and impaired, guarantee the security of self-burning coke cleaning, must carry out innoxious self-burning coke cleaning by manual control, its concrete steps are as follows:
Feed liquid discharging in the heater 1 feed liquid heated passage 8 totally and with feed liquid heated passage entrance 11 and feed liquid heated passage outlet 6 is in communication with the outside.
By heat carrier in the 7 interior mobile heat releases of heat carrier heat release passage, and constantly carry out incremental intensification and regulate, make the liquid phase component among the feed liquid heated passage 8 interior coking materials be evaporated release, when evaporation release is complete, in the situation that oxygen participates in, the temperature of coking material will constantly rise to it more than ignition temperature.Both can make by the temperature that surmounts self-ignition point coking material enter self-burning heat release state this moment, also can utilize blowtorch that flame is sprayed on the coking material in the feed liquid heated passage coking material lighted by feed liquid heated passage entrance and make coking material enter self-burning heat release state.
Continue flowing in heat carrier heat release passage 7 by heat carrier, with feed liquid heated passage 8 interior coking materials because of the absorption of flowing of the heat that discharges of burning, make the heater 1 of this moment be in reverse heat absorption state, the heat carrier of this moment not only no longer needs extraneous heating combined equipment for its heating, can also carry out suitable heat release with hot equipment to other.
By the heat carrier exhaust temperature of monitoring heat carrier heat release channel outlet 5 and feed liquid heated passage outlet 6 and the heat release degree that the thermal current exhaust temperature is understood its self-burning.
By the air demand at manual control feed liquid heated passage entrance 11 places, the heat that coking material is discharged in the self-burning process further is controlled in the temperature range that heater 1 can bear.
One of method of control air demand is: in order the self-burning phenomenon to be maintained slowly and don't the relative low temperature heat release state that extinguishes, gas supply regulation is originally stated the minimum state that needs to keeping.
Two of the method for control air demand is: be discharged into the external world for the heat that the self-burning phenomenon is discharged carries it with relative maximization air-flow, gas supply regulation is originally stated the maximum rating that needs to keeping, equipped air blast outside feed liquid passage end opening.
In order further to improve environmental protection level, the thermal current mixture that feed liquid heated passage outlet 6 is outwards discharged is introduced in the combustion chamber of boiler, it is fully burnt.
The description of above-described embodiment all is not the restriction to the present invention program, any according to the present invention design done only for pro forma but not substantial equivalent transformation all should be considered as technical scheme category of the present invention.
Claims (10)
- One kind the decompression short course distillation device, comprise evaporimeter, feeding mechanism, feed liquid heating arrangements, the distillate cooling collection mechanism of decompressor, it is characterized in that: the heater in the described feed liquid heating arrangements is the double passage heat exchanger that is arranged at outside the evaporimeter, a passage in this double passage heat exchanger is the feed liquid heated passage, its feed liquid heated passage entrance is communicated with the feed liquid floss hole of evaporimeter by be heated feed liquid intake pipeline and feed liquid delivery pump, and its feed liquid heated passage outlet is communicated with the high-order feed liquid evaporation channel entrance of evaporimeter by the feed liquid export pipeline that is heated; Another passage in this double passage heat exchanger is heat carrier heat release passage, and its import and export is communicated with the heat carrier pipeloop.
- 2. described decompression short course distillation device according to claim 1, it is characterized in that: described double passage heat exchanger is a binary channels tubular heat exchanger.
- 3. described decompression short course distillation device according to claim 2 is characterized in that: be provided with FlexbleJoint on the outer cylinder body of described binary channels tubular heat exchanger.
- 4. described decompression short course distillation device according to claim 1 is characterized in that: on the feed liquid intake pipeline that is heated between the feed liquid heated passage entrance of described heater and the feed liquid delivery pump check valve is installed.
- 5. described decompression distillation heater according to claim 1 is characterized in that: on the feed liquid export pipeline that is heated between the feed liquid heated passage outlet of described heater and the high-order feed liquid evaporation channel entrance of evaporimeter barostat is installed.
- 6. the spontaneous combustion coke cleaning method of the heater of the short course distillation device that reduces pressure as claimed in claim 1, its step is as follows:A. with the discharging of the feed liquid in the feed liquid heated passage of heater totally, and with feed liquid heated passage entrance and the outlet of feed liquid heated passage be in communication with the outside;B. pass into more than 100 ℃ the heat carrier heat release of flowing in the heat carrier heat release passage, and more than the temperature to 200 of incremental rising heat carrier ℃, make that the liquid phase component among the coking material is evaporated release in the feed liquid heated passage, when evaporation release is complete, the temperature of coking material will constantly rise, by spontaneous combustion or light and make it enter burning heat release state;C. continue in heat carrier heat release passage, to pass into heat carrier, flow by the lasting of heat carrier, with coking material in the feed liquid heated passage because of the absorption of flowing of the heat that discharges of burning, make the heater of this moment be in reverse heat absorption state, the heat carrier of this moment not only no longer needs extraneous heating combined equipment for its heating, can also carry out suitable heat release with hot equipment to other;D. monitor heat carrier exhaust temperature and the thermal current exhaust temperature of the outlet of heat carrier heat release channel outlet and feed liquid heated passage, understand the heat release degree of its self-burning, the air demand of control feed liquid heated passage porch, the heat that coking material is discharged in spontaneous combustion process further are controlled in the combustion reference temperature that heater can bear.
- 7. the spontaneous combustion coke cleaning method of the heater of described decompression short course distillation device according to claim 6, it is characterized in that: the method for control air demand is in the described steps d: in order dieseling to be maintained slowly and don't the relative low temperature heat release state that extinguishes, gas supply regulation is originally stated the minimum state that needs to keeping.
- 8. the spontaneous combustion coke cleaning method of the heater of described decompression short course distillation device according to claim 6, it is characterized in that: the method for control air demand is in the described steps d: be discharged into the external world for the heat that dieseling is discharged carries it with relative maximization air-flow, gas supply regulation is originally stated the maximum rating that needs to keeping, be equipped with air blast at feed liquid heated passage entrance.
- 9. the spontaneous combustion coke cleaning method of the heater of described decompression short course distillation device according to claim 6 is characterized in that: described feed liquid heated passage outlet is equipped with and connects boiler furnace and to the thermal current conveyance conduit of boiler furnace discharging thermal current.
- 10. the spontaneous combustion coke cleaning method of the heater of described decompression short course distillation device according to claim 6, it is characterized in that: the method for lighting coking material among the described step b is: with blowtorch flame is sprayed on the coking material in the feed liquid heated passage by feed liquid heated passage entrance.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210323001.0A CN102861450B (en) | 2012-09-04 | 2012-09-04 | Reduced-pressure short-path distilling device and spontaneous combustion decoking method of heater of reduced-pressure short-path distilling device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210323001.0A CN102861450B (en) | 2012-09-04 | 2012-09-04 | Reduced-pressure short-path distilling device and spontaneous combustion decoking method of heater of reduced-pressure short-path distilling device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102861450A true CN102861450A (en) | 2013-01-09 |
| CN102861450B CN102861450B (en) | 2014-08-20 |
Family
ID=47440749
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210323001.0A Expired - Fee Related CN102861450B (en) | 2012-09-04 | 2012-09-04 | Reduced-pressure short-path distilling device and spontaneous combustion decoking method of heater of reduced-pressure short-path distilling device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102861450B (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1128185A (en) * | 1967-02-03 | 1968-09-25 | Gni I Pi Azotnoi Promy Iproduk | A unit for batchwise vacuum rectification of heat sensitive liquid mixtures under forced circulations |
| WO1991011238A1 (en) * | 1990-02-02 | 1991-08-08 | Sports Marine International Pty. Ltd. | Vacuum distillation using suction apparatus |
| US5980695A (en) * | 1996-11-14 | 1999-11-09 | Transglobal Industrial Services, Inc. | Apparatus for vacuum distillation of solvents |
| JP2005021745A (en) * | 2003-06-30 | 2005-01-27 | Rikogaku Shinkokai | Distillation apparatus and reaction device |
| CN201216884Y (en) * | 2008-06-26 | 2009-04-08 | 青岛光大装备科技有限公司 | Energy-conservation forced-air circulation liquid extract concentrating device |
| CN202762118U (en) * | 2012-09-04 | 2013-03-06 | 吴国存 | Pressure-reduction and short-range distillation apparatus |
-
2012
- 2012-09-04 CN CN201210323001.0A patent/CN102861450B/en not_active Expired - Fee Related
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1128185A (en) * | 1967-02-03 | 1968-09-25 | Gni I Pi Azotnoi Promy Iproduk | A unit for batchwise vacuum rectification of heat sensitive liquid mixtures under forced circulations |
| WO1991011238A1 (en) * | 1990-02-02 | 1991-08-08 | Sports Marine International Pty. Ltd. | Vacuum distillation using suction apparatus |
| US5980695A (en) * | 1996-11-14 | 1999-11-09 | Transglobal Industrial Services, Inc. | Apparatus for vacuum distillation of solvents |
| JP2005021745A (en) * | 2003-06-30 | 2005-01-27 | Rikogaku Shinkokai | Distillation apparatus and reaction device |
| CN201216884Y (en) * | 2008-06-26 | 2009-04-08 | 青岛光大装备科技有限公司 | Energy-conservation forced-air circulation liquid extract concentrating device |
| CN202762118U (en) * | 2012-09-04 | 2013-03-06 | 吴国存 | Pressure-reduction and short-range distillation apparatus |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102861450B (en) | 2014-08-20 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101907294B (en) | Low-NOx combustion method of cyclone furnace and liquid slag waste heat recycling system of cyclone furnace | |
| CN102648039B (en) | For removing the method and apparatus of VOC from air-flow | |
| CN102242946A (en) | Concentrated heat supply system for reclaiming smoke afterheat by absorption heat pump | |
| CN106765009B (en) | Continuous heat accumulating and burning gas heat pipe steam generator and method for comprehensively recovering waste heat of flue gas | |
| CN202581340U (en) | Smoke-free boiler for treating municipal refuse | |
| CN202762118U (en) | Pressure-reduction and short-range distillation apparatus | |
| CN101858646B (en) | Energy-saving and environment-protection heating device for distillation of oily waste materials | |
| CN201819396U (en) | Energy-saving and environmentally-friendly heating device for distilling oily waste | |
| CN102221198B (en) | Low NOx combustion method for cyclone furnace and liquid state slagging and afterheat recycling system for cyclone furnace | |
| CN102861450B (en) | Reduced-pressure short-path distilling device and spontaneous combustion decoking method of heater of reduced-pressure short-path distilling device | |
| CN103759467A (en) | Two-section smoke hot water single-dual effect composite lithium bromide absorption refrigerating unit | |
| CN102997251A (en) | Liquid waste and exhaust gas recycling system for chemical by-products | |
| CN202692101U (en) | Vehicular oil burning boiler and tail inert gas purification equipment | |
| CN2769759Y (en) | Energy-saving water bath heater | |
| CN202675614U (en) | High-temperature vacuum superconducting phase-change heating furnace | |
| CN100549553C (en) | Taking-out back water reciprocating flue type boiler | |
| CN212419085U (en) | Drawer type box thermal desorption system for soil remediation | |
| CN105299606B (en) | Temperature difference water inlet waste heat circulation boiler | |
| CN102853433A (en) | Movable urban garbage treatment residue heat recycling device | |
| CN207871853U (en) | A kind of bitumen flue gas comprehensive purifying processing unit | |
| CN103090381B (en) | Burner | |
| CN101556078A (en) | Special heating medium furnace for oil field gathering and transportation pipeline | |
| CN204853423U (en) | Use full -automatic steam generation equipment of alcohol group fuel | |
| CN202868697U (en) | Chemical industry secondary product waste liquid and exhaust gas recycling system | |
| CN110938739A (en) | Heat treatment equipment with recyclable waste heat |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140820 |