CN206457433U - A kind of equipment of hydrocarbon partial oxidation production acetylene and synthesis gas - Google Patents
A kind of equipment of hydrocarbon partial oxidation production acetylene and synthesis gas Download PDFInfo
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- CN206457433U CN206457433U CN201621409789.7U CN201621409789U CN206457433U CN 206457433 U CN206457433 U CN 206457433U CN 201621409789 U CN201621409789 U CN 201621409789U CN 206457433 U CN206457433 U CN 206457433U
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- partial oxidation
- synthesis gas
- reative cell
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- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 title claims abstract description 56
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 title claims abstract description 55
- 230000003647 oxidation Effects 0.000 title claims abstract description 43
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 43
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 40
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 40
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 38
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 38
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 38
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 37
- 238000010791 quenching Methods 0.000 claims abstract description 52
- 230000000171 quenching effect Effects 0.000 claims abstract description 52
- 238000001816 cooling Methods 0.000 claims abstract description 42
- 238000006243 chemical reaction Methods 0.000 claims description 6
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 239000007789 gas Substances 0.000 description 76
- 238000000034 method Methods 0.000 description 32
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Natural products C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 23
- 229910052760 oxygen Inorganic materials 0.000 description 21
- 239000001301 oxygen Substances 0.000 description 21
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 20
- 230000008569 process Effects 0.000 description 20
- 238000005336 cracking Methods 0.000 description 18
- 239000003345 natural gas Substances 0.000 description 16
- 239000006229 carbon black Substances 0.000 description 7
- 230000000694 effects Effects 0.000 description 7
- -1 oxygen Hydrocarbon Chemical class 0.000 description 6
- 239000007921 spray Substances 0.000 description 6
- 239000002918 waste heat Substances 0.000 description 6
- 230000008901 benefit Effects 0.000 description 5
- 239000006227 byproduct Substances 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- IHICGCFKGWYHSF-UHFFFAOYSA-N C1=CC=CC=C1.CC1=CC=CC=C1.CC1=CC=CC=C1C Chemical group C1=CC=CC=C1.CC1=CC=CC=C1.CC1=CC=CC=C1C IHICGCFKGWYHSF-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- XTXRWKRVRITETP-UHFFFAOYSA-N Vinyl acetate Chemical compound CC(=O)OC=C XTXRWKRVRITETP-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 150000001345 alkine derivatives Chemical class 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000035807 sensation Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses the equipment of a kind of hydrocarbon partial oxidation production acetylene and synthesis gas, including the blender being sequentially connected（3）, reative cell（5）, cooling chamber（16）, cooling device and separator（17）, it is characterised in that：In the cooling device and the separator（17）Between be provided with and the reative cell（5）The branch road of the quenching gas of bottom connection, compressor is provided with the branch road（12）.The equipment that acetylene and synthesis gas are produced using hydrocarbon partial oxidation of the present utility model, can reduce energy consumption, good economy performance.
Description
Technical field
The equipment that the utility model is related to a kind of hydrocarbon partial oxidation acetylene and synthesis gas.
Background technology
Acetylene is a kind of very important basic chemical industry raw material, is widely used in the life of vinyl acetate, BDO etc.
Production；Synthesis gas is then the important source material for producing methanol, ethylene glycol and its downstream product.The main production process of natural gas acetylene
There are arc process, partial oxidation process, plasma method etc., wherein arc process and plasma method because power consumption is big, more severe to equipment requirement
Carve, popularization and application are difficult to so far.Partial oxidation process has the advantages that energy consumption is low, it is small to pollute, and is West Europe and north america production second
The main method of alkynes.In the process, hydrocarbon is preheated to 300~650 DEG C respectively with oxygen, and heating will be significantly improved more than 650 DEG C
The material requirement of equipment, while hydrocarbon can crack analysis carbon more than 650 DEG C.By diffuser after being sufficiently mixed in gas mixer
Into acetylene reaction stove combustion chamber, the water spray or oil quenching is cold that the cracking containing acetylene is obtained with terminating reaction after several milliseconds are reacted
Gas, cracking gas can obtain acetylene and synthesis gas by solvent absorption and parsing.
Partial oxidation reactor quenching industrially uses water quenching cold and the cold two kinds of technique of oil quenching.The cold advantage of water quenching is that quenching effect is good,
The temperature of high-temperature reacting gas promptly can be down to 80 ~ 90 DEG C from 1500 DEG C or so, so as to ensure that higher acetylene is received
Rate, therefore, cold water quenching is most popular quenching method.But spray water quenching there is also it is more the problem of, firstly, because charcoal
Heisui River temperature only has 80 ~ 90 DEG C, and a large amount of heat energy contained in sooty water are because hot quality is too low and is difficult with, even if water quenching is cold
Higher temperature is controlled afterwards, because substantial amounts of heat is in the heat of transformation of water, is equally low-quality heat, is caused waste heat largely to waste；
Secondly, sooty water has carbon black and aromatic hydrocarbon substance to evaporate in the device such as carbon black tank and cooling tower region, causes serious sky
Gas pollutes；Because cooling tower is open cooling, water evaporation loss height is larger, causes water resource waste in short supply；Open carbon black
Water cooling mode causes environmental pollution.So, it is low to there is heat of reaction utilization rate in the cold technique of water quenching（Efficiency about 60%）, energy consumption
The problems such as height, environmental pollution and serious water resource waste.
The cold technique of oil quenching is to utilize the cold pyroreaction gas of oil quenching, byproduct steam or the technique for producing other products, can be effective
Reclaim gas by partial oxidation of natural produce high temperature preheating, with preferable economic benefit and social benefit.BASF Corp. of Germany
Start the sixties in last century to use the cold technique of oil quenching always, so far, only BASF AG is in Ludwigshafen
（Ludwigshafen）The industrialization of the cold technique of oil quenching is realized, residual oil quenching, by-product light aromatics BTX is utilized（Benzene-toluene-
Xylene mixture, Benzene-Toluene-Xylene）.Chongqing City Chemical Engineering Inst. of China develops day the nineties in last century
Right gas acetylene oil spout quenching technology, establishes lab scale and pilot-plant, using condensate quenching by-product ethene, its complex process,
So far industrialization is not yet realized.Although the cold recyclable portion of energy of oil quenching, its cracked gas complicated components, add separating technology
Complexity.
The chilling and heat recovery of a kind of gas by partial oxidation of natural process are disclosed in Chinese patent CN102329189A
Method and device, the device include blender, combustion chamber, hot mixture guiding device, heat exchanger, separator, in institute
State and quenching branch road is provided between separator and the combustion chamber.Using the gas by partial oxidation of natural process in above-mentioned patent
Chilling and heat reclaim unit, in actual use, can consume substantial amounts of energy, the energy of consumption in separation process
No less than the heat of collection, and the concentration of acetylene collected using the patent is low.
Utility model content
The purpose of this utility model is to provide a kind of energy consumption low, economical hydrocarbon partial oxidation production acetylene and synthesis gas
Equipment.
To achieve these goals, the utility model is realized in：A kind of hydrocarbon partial oxidation production acetylene and synthesis
The equipment of gas, including blender, reative cell, cooling chamber, cooling device and the separator being sequentially connected, it is characterised in that：Institute
The branch road that the quenching gas being connected with the reative cell bottom is provided between cooling device and the separator is stated, in the branch road
On be provided with compressor.The hydrocarbon partial oxidation production acetylene and the equipment of synthesis gas set using aforesaid way, can save energy
Consumption, good economy performance.And the concentration of acetylene produced using the equipment is high.Wherein, the compressor can be screw rod, centrifugation pressure
Contracting machine, preferably helical-lobe compressor.
In order to further improve cooling effect, it is provided with one end being connected with the reative cell bottom of the branch road many
Bar jet pipe, the spout of the jet pipe is connected with the bottom side of the wall of the reative cell and communicated with the reactor chamber.
Save cool time to further improve cooling effect, the spout of the jet pipe is rounded, oval, rectangle,
Triangle etc., it is preferably oval.
In order to further improve cooling effect, the axis of the major axis of the spout and the reative cell has 45-90 °
Included angle B.
In order to further improve cooling effect, the cross section of the reative cell is hexagon, octagon, 12 deformations, circle
Shape or ellipse etc., it is preferably oval.
In order to further save cool time, the jet pipe is 4-16 roots and set along the reative cell periphery wall.
It is preferred that, the jet pipe is 6 and is uniformly arranged along the reative cell periphery wall.
In order to further improve cooling effect, the axis of the jet pipe and the axis of the reative cell have 100-
165 ° of included angle A.
It is preferred that, the axis of the axis of the jet pipe and the reative cell has 145 ° of included angle A.
In order to further save energy consumption, the cooling device includes first-class heat exchanger and the institute being connected with the cooling chamber
The cooling tower stated the secondary heat exchanger of first-class heat exchanger connection and be connected with the secondary heat exchanger.
The quenching equipment of acetylene and synthesis gas is produced using hydrocarbon partial oxidation of the present utility model, with following beneficial effect
Really：
1. good energy-conserving effect, good economy performance.Acetylene per ton can 8-9 tons of by-product high-pressure steam, substantially reduce acetylene production into
This, remarkable in economical benefits.
2. heat of reaction is effectively utilized, and obtain the black product of by-product dry carbon of high-quality, carbon black clearance 99% with
On.
3. system does not introduce new impurity, the loss of During Quenching acetylene is small, and concentration of acetylene is cold quite with water quenching, to follow-up point
From purification without influence.
4. good cooling results, technology is environment-friendly.Air quenching is cold do not produce water quenching refrigeration technique need it is substantial amounts of containing organic
Volatile component sooty water, greatly reduces volatile matter VOC emission.
5. generate polymer in reduction system, it is ensured that system long-term operation.
Brief description of the drawings
Fig. 1 is the equipment flowsheet of hydrocarbon partial oxidation production acetylene and synthesis gas in the embodiment of the present invention；
Fig. 2 is the connection diagram of jet pipe and reative cell in the embodiment of the present invention；
Fig. 3 is the jet pipe mouth of pipe and the location arrangements schematic diagram of reative cell axis in the embodiment of the present invention.
Embodiment
The utility model will be introduced by the embodiment shown in accompanying drawing below, but the utility model is not limited to institute
The embodiment of introduction, any improvement or replacement on the present embodiment essence spirit still falls within the utility model claim
Scope claimed：
Embodiment：As Figure 1-3, a kind of equipment of hydrocarbon partial oxidation production acetylene and synthesis gas, including be sequentially connected
Blender 3, reative cell 5, cooling chamber 16, cooling device and separator 17, the cooling device and the separator 17 it
Between be provided with the branch road of the quenching gas being connected with the bottom of reative cell 5, compressor 12 is provided with the branch road.Wherein,
The compressor can be screw rod or centrifugal compressor, and centrifugal compressor is used in the present embodiment.
Wherein, one end being connected with the bottom of reative cell 5 of the branch road is provided with a plurality of jet pipe 6, the jet pipe 6
Spout 62 be connected and communicated with the cavity of reative cell 5 with the bottom side of the wall of the reative cell 5.And the spray of the jet pipe 6
Mouth 62 is oval, and the axis 31 of the major axis 63 of the spout 62 and the reative cell 5 has 45-90 ° of included angle A 61.Should
Included angle A 61 can select singly to be not limited to 45 °, 50 °, 55 °, 60 °, 65 °, 70 °, 75 °, 80 °, 85 °, 90 °.
In addition, the jet pipe 6 is 4-16 roots and set along the reative cell periphery wall.The jet pipe 6 can select single 4,
5th, 6,7,8,9,10,11,12,13,14,15 or 16.
In order to further improve cooling effect, the axis of the jet pipe 6 has 100- with the axis of the reative cell
165 ° of included angle B 64.The included angle B 64 can select singly to be not limited to：100°、105°、110°、115°、120°、125°、130°、
135 °, 140 °, 145 °, 150 °, 155 °, 160 ° or 165 °.Moreover, the cross section of the reative cell 5 is circular, ellipse, it is many
Side shape etc., in the present embodiment, the cross section of the reative cell 5 is ellipse.
Moreover, the cooling device includes the first-class heat exchanger being connected with the cooling chamber 16 and the first-class heat exchanger
The secondary heat exchanger of connection and the cooling tower 11 being connected with the secondary heat exchanger.In the present embodiment, the one-level heat exchange
Device is that waste heat boiler 8, the secondary heat exchanger are boiler water heater 10, in the first-class heat exchanger and the secondary heat exchanger
Between be additionally provided with deduster 9, the deduster 9 is used to remove the carbon black inside cracking gas.
In process of production, oxygen 1 and hydrocarbon 2 are preheating to 300-650 DEG C, the volume ratio of oxygen 1 and hydrocarbon 2 by heater
Control is between 0.4-0.7, and operating pressure is 0.1-0.4Mpa, and the high temperature, hydrocarbon and oxygen after preheating are passed into the blender 3
It is interior quick well mixed, then pass in the reative cell 5, mixed gas is entered by the multi-port burner plate 4 in reative cell 5
Row combustion reaction, burner plate 4 is provided with auxiliary oxygen, and stable flame, flame temperature reaches 1300-1500 DEG C, and actual temp is by oxygen
Hydrocarbon is than determining.Reaction time passes through several milliseconds, in the bottom of reative cell 5 by the jet pipe 6 to the high temperature generated after combustion reaction
Cracking gas carries out the temperature of cracking gas 7 after quenching, quenching for 400-800 DEG C and then is passed into cooling chamber 16.Cooling chamber 16
Interior cracking gas 7 drops to 300-400 DEG C by the waste heat boiler 8, and the heat consumed is used for waste heat boiler 8 and produces overheat
Steam 15, the cracking gas come out from the waste heat boiler 8 is removing the carbon black in cracking gas by the deduster 9, forms secondary
Product.Remove the cracking gas after carbon black and passing through the heating boiler water 14 of boiler water heater 10 so that cracking gas temperature drops
To 80-200 DEG C, and the heat consumed is used to produce high-temperature boiler water, and the high-temperature boiler water is passed into the waste heat boiler 8
For producing superheated steam 15.Cracking gas in from the boiler water heater 10 out drops to 20- by the cooling tower 11
80 DEG C, obtain normal temperature cracking gas 13.The part of normal temperature cracking gas 13 come out from the cooling tower 11 passes through the quenching branch road
Quenching is carried out to the Pintsch process gas after compression, another part isolates acetylene and synthesis gas by the separator 17.
In the present embodiment, using natural gas and oxygen production acetylene and synthesis gas, first, natural gas is passed through with oxygen
Heater is preheating to 650 DEG C, and the volume ratio control of oxygen and natural gas is 0.55, and the operating pressure of blender 3 is 0.1Mpa,
The cross section of reative cell 5 is using ellipse, and quenching atmospheric pressure is 0.2Mpa, using four jet pipes 6, the jet pipe 6 and the reaction
The axis 51 of room 5 forms 145 ° of included angle A 61 so that quenching gas and Pintsch process gas in 145 ° it is reverse spray into, and described quench
The gas velocity ratio of cold air and the Pintsch process gas is that the temperature of cracking gas 7 is 600 DEG C after 2.5, quenching, is passed through warm after two-stage heat exchanger
Spend for 90 DEG C.Obtained cracked gas concentration of acetylene is 8%（mol）, partial oxidation reactor heat utilization ratio raising 15%.
In another embodiment, using natural gas and oxygen production acetylene and synthesis gas, first, natural gas is led to oxygen
Cross heater and be preheating to 650 DEG C, the volume ratio control of oxygen and natural gas is 0.55, and the operating pressure of blender 3 is
0.1Mpa, the cross section of reative cell 4 is using circle, and quenching atmospheric pressure is 0.2Mpa, using four jet pipes 5, the jet pipe 5 and institute
The axis 51 for stating reative cell 5 forms 120 ° of included angle A 61 so that quenching gas is inversely sprayed into Pintsch process gas in 120 °, and
The gas velocity ratio of the quenching gas and the Pintsch process gas is that the temperature of cracking gas 7 is 600 DEG C after 2.5, quenching, is exchanged heat by two-stage
Temperature is 90 DEG C after device.Obtained cracked gas concentration of acetylene is 7.8%（mol）, partial oxidation reactor heat utilization ratio raising 15%.
In another embodiment, using natural gas and oxygen production acetylene and synthesis gas, first, natural gas is led to oxygen
Cross heater and be preheating to 650 DEG C, the volume ratio control of oxygen and natural gas is 0.54, and the operating pressure of blender 3 is
0.3Mpa, the cross section of reative cell 5 uses hexagon, and quenching atmospheric pressure is 0.3Mpa, using four jet pipes, the jet pipe 6 with
The axis 51 of the reative cell 5 forms 145 ° of included angle A 61 so that quenching gas is inversely sprayed into Pintsch process gas in 145 °,
And the gas velocity ratio of the quenching gas and the Pintsch process gas is that the temperature of cracking gas 7 is 600 DEG C after 2.5, quenching, is changed by two-stage
Temperature is 120 DEG C after hot device.Obtained cracked gas concentration of acetylene is 7.9%（mol）, partial oxidation reactor heat utilization ratio raising 14.8%.
In another embodiment, using natural gas and oxygen production acetylene and synthesis gas, first, natural gas is led to oxygen
Cross heater and be preheating to 650 DEG C, the volume ratio control of oxygen and natural gas is 0.55, and the operating pressure of blender 3 is
0.1Mpa, the cross section of reative cell 5 uses octagon, and quenching atmospheric pressure is 0.2Mpa, using six roots of sensation jet pipe 6, the jet pipe 6 with
The axis 51 of the reative cell 5 forms 145 ° of included angle A 61 so that quenching gas is inversely sprayed into Pintsch process gas in 145 °,
And the gas velocity ratio of the quenching gas and the Pintsch process gas is that the temperature of cracking gas 7 is 600 DEG C after 2.5, quenching, is changed by two-stage
Temperature is 90 DEG C after hot device.Obtained cracked gas concentration of acetylene is 7.9%（mol）, partial oxidation reactor heat utilization ratio raising 15%.
In another embodiment, using natural gas（Wherein ethane 20%（mol））With oxygen production acetylene and synthesis gas, head
First, natural gas and oxygen are preheating to 580 DEG C by heater, the volume ratio control of oxygen and natural gas is in 0.65, blender
3 operating pressure is 0.1Mpa, and the cross section of reative cell 5 uses dodecagon, and quenching atmospheric pressure is 0.2Mpa, using four sprays
The axis 51 of pipe 6, the jet pipe 6 and the reative cell 5 forms 135 ° of included angle A 61 so that quenching gas and Pintsch process gas
In 135 ° it is reverse spray into, and the gas velocity ratio of the quenching gas and the Pintsch process gas is that the temperature of cracking gas 7 is after 2.3, quenching
600 DEG C, be 90 DEG C by temperature after two-stage heat exchanger.Obtained cracked gas concentration of acetylene is 9.6%（mol）, partial oxidation reactor heat profit
14.5% is improved with rate.
Claims (21)
1. the equipment of a kind of hydrocarbon partial oxidation production acetylene and synthesis gas, including the blender being sequentially connected（3）, reative cell（5）、
Cooling chamber（16）, cooling device and separator（17）, it is characterised in that：In the cooling device and the separator（17）Between
It is provided with and the reative cell（5）The branch road of the quenching gas of bottom connection, compressor is provided with the branch road（12）.
2. the equipment of hydrocarbon partial oxidation production acetylene as claimed in claim 1 and synthesis gas, it is characterised in that：In the branch road
The one end being connected with the reative cell bottom be provided with a plurality of jet pipe（6）, the jet pipe（6）Spout（62）With the reaction
Room（5）Bottom side of the wall connection and with the reative cell（5）Cavity is communicated.
3. the equipment of hydrocarbon partial oxidation production acetylene as claimed in claim 2 and synthesis gas, it is characterised in that：The jet pipe
（6）Spout（62）It is oval.
4. the equipment of hydrocarbon partial oxidation production acetylene as claimed in claim 3 and synthesis gas, it is characterised in that：The spout
（62）Major axis（63）With the reative cell（5）Axis（51）With 45-90 ° of included angle B（64）.
5. the equipment of hydrocarbon partial oxidation production acetylene as claimed in claim 1 and synthesis gas, it is characterised in that：The reative cell
（5）Cross section be hexagon, octagon, 12 deformations, circular or ellipse.
6. the equipment of the hydrocarbon partial oxidation production acetylene and synthesis gas as described in claim 2,3 or 4, it is characterised in that：It is described
Reative cell（5）Cross section be hexagon, octagon, 12 deformations, circular or ellipse.
7. the equipment of the hydrocarbon partial oxidation production acetylene and synthesis gas as described in claim 2,3 or 4, it is characterised in that：It is described
Jet pipe（6）For 4-16 roots and along the reative cell（5）Periphery wall is set.
8. the equipment of hydrocarbon partial oxidation production acetylene as claimed in claim 6 and synthesis gas, it is characterised in that：The jet pipe
（6）For 4-16 roots and along the reative cell（5）Periphery wall is set.
9. the equipment of hydrocarbon partial oxidation production acetylene as claimed in claim 7 and synthesis gas, it is characterised in that：The jet pipe
（6）For 6 and along the reative cell（5）Periphery wall is uniformly arranged.
10. the equipment of hydrocarbon partial oxidation production acetylene as claimed in claim 8 and synthesis gas, it is characterised in that：The jet pipe
（6）For 6 and along the reative cell（5）Periphery wall is uniformly arranged.
11. the equipment of hydrocarbon partial oxidation production acetylene as claimed in claim 7 and synthesis gas, it is characterised in that：The jet pipe
（6）Axis and the reative cell（5）Axis（51）With 100-165 ° of included angle A（61）.
12. the equipment of hydrocarbon partial oxidation production acetylene as claimed in claim 8 and synthesis gas, it is characterised in that：The jet pipe
（6）Axis and the reative cell（5）Axis（51）With 100-165 ° of included angle A（61）.
13. the equipment of hydrocarbon partial oxidation production acetylene as claimed in claim 9 and synthesis gas, it is characterised in that：The jet pipe
（6）Axis and the reative cell（5）Axis（51）With 100-165 ° of included angle A（61）.
14. the equipment of hydrocarbon partial oxidation production acetylene as claimed in claim 10 and synthesis gas, it is characterised in that：The jet pipe
（6）Axis and the reative cell（5）Axis（51）With 100-165 ° of included angle A（61）.
15. the equipment of hydrocarbon partial oxidation production acetylene as claimed in claim 11 and synthesis gas, it is characterised in that：The jet pipe
（6）Axis and the reative cell（5）Axis（51）With 145 ° of included angle A（61）.
16. the equipment of hydrocarbon partial oxidation production acetylene as claimed in claim 12 and synthesis gas, it is characterised in that：The jet pipe
（6）Axis and the reative cell（5）Axis（51）With 145 ° of included angle A（61）.
17. the equipment of hydrocarbon partial oxidation production acetylene as claimed in claim 13 and synthesis gas, it is characterised in that：The jet pipe
（6）Axis and the reative cell（5）Axis（51）With 145 ° of included angle A（61）.
18. the equipment of hydrocarbon partial oxidation production acetylene as claimed in claim 14 and synthesis gas, it is characterised in that：The jet pipe
（6）Axis and the reative cell（5）Axis（51）With 145 ° of included angle A（61）.
19. the equipment of hydrocarbon partial oxidation production acetylene as claimed in claim 6 and synthesis gas, it is characterised in that：The cooling
Equipment includes and the cooling chamber（16）The first-class heat exchanger of connection, the secondary heat exchanger being connected with the first-class heat exchanger and
The cooling tower being connected with the secondary heat exchanger（11）.
20. the equipment of hydrocarbon partial oxidation production acetylene as claimed in claim 7 and synthesis gas, it is characterised in that：The cooling
Equipment includes and the cooling chamber（16）The first-class heat exchanger of connection, the secondary heat exchanger being connected with the first-class heat exchanger and
The cooling tower being connected with the secondary heat exchanger（11）.
21. the hydrocarbon partial oxidation life as described in claim 1,2,3,4,5,8,9,10,11,12,13,14,15,16,17 or 18
The equipment for producing acetylene and synthesis gas, it is characterised in that：The cooling device includes and the cooling chamber（16）The one-level of connection is changed
Hot device, the secondary heat exchanger being connected with the first-class heat exchanger and the cooling tower being connected with the secondary heat exchanger（11）.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621409789.7U CN206457433U (en) | 2016-12-21 | 2016-12-21 | A kind of equipment of hydrocarbon partial oxidation production acetylene and synthesis gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621409789.7U CN206457433U (en) | 2016-12-21 | 2016-12-21 | A kind of equipment of hydrocarbon partial oxidation production acetylene and synthesis gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206457433U true CN206457433U (en) | 2017-09-01 |
Family
ID=59697127
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201621409789.7U Active CN206457433U (en) | 2016-12-21 | 2016-12-21 | A kind of equipment of hydrocarbon partial oxidation production acetylene and synthesis gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206457433U (en) |
-
2016
- 2016-12-21 CN CN201621409789.7U patent/CN206457433U/en active Active
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