CN203700291U - Gasification furnace for synthetic natural gas - Google Patents
Gasification furnace for synthetic natural gas Download PDFInfo
- Publication number
- CN203700291U CN203700291U CN201320731815.8U CN201320731815U CN203700291U CN 203700291 U CN203700291 U CN 203700291U CN 201320731815 U CN201320731815 U CN 201320731815U CN 203700291 U CN203700291 U CN 203700291U
- Authority
- CN
- China
- Prior art keywords
- furnace body
- furnace
- gasification
- coal
- natural gas
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- 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.)
- Expired - Lifetime
Links
- 238000002309 gasification Methods 0.000 title claims abstract description 35
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title description 23
- 239000007789 gas Substances 0.000 claims abstract description 53
- 239000001257 hydrogen Substances 0.000 claims abstract description 34
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 34
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 33
- 239000003345 natural gas Substances 0.000 claims abstract description 19
- 238000002347 injection Methods 0.000 claims abstract description 10
- 239000007924 injection Substances 0.000 claims abstract description 10
- 239000000571 coke Substances 0.000 claims abstract 6
- 239000002994 raw material Substances 0.000 claims abstract 2
- 239000011819 refractory material Substances 0.000 claims description 5
- 239000000428 dust Substances 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract 1
- 239000006200 vaporizer Substances 0.000 description 29
- 239000003245 coal Substances 0.000 description 22
- 239000000047 product Substances 0.000 description 16
- 238000000034 method Methods 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 10
- 238000005984 hydrogenation reaction Methods 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 3
- 239000007790 solid phase Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000013459 approach Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000013618 particulate matter Substances 0.000 description 2
- 238000011020 pilot scale process Methods 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 239000012265 solid product Substances 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 238000012795 verification Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- -1 between dividing Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 150000003254 radicals Chemical class 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Landscapes
- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
一种用于煤制天然气的气化炉是由炉体（1）、进料喷嘴（3）、气化室（2）、半焦收集池（7）组成，其特征在于炉体（1）分为上、中、下三部分，炉体（1）上部分为垂直段，炉体（1）中部分为扩大段（6），炉体（1）下部分为V字形半焦收集池（7），炉体（1）上部分为气化室（2），进料喷嘴（3）位于气化室（2）的顶端，在气化室（2）和炉体（1）上部分之间设置有对原料气预热的盘管换热器（8），盘管换热器（8）上方的炉体（1）设有产品气出口（11），炉体（1）扩大段（6）的下部设有高压气喷吹管（5），半焦收集池（7）的底部设有排料口（12）。本实用新型具有耗能低、氢耗量小，除尘负荷轻的优点。
A gasification furnace for coal-to-natural gas is composed of a furnace body (1), a feed nozzle (3), a gasification chamber (2), and a semi-coke collection pool (7), and is characterized in that the furnace body (1) Divided into upper, middle and lower parts, the upper part of the furnace body (1) is a vertical section, the middle part of the furnace body (1) is an enlarged section (6), and the lower part of the furnace body (1) is a V-shaped semi-coke collection pool ( 7), the upper part of the furnace body (1) is the gasification chamber (2), the feed nozzle (3) is located at the top of the gasification chamber (2), between the gasification chamber (2) and the upper part of the furnace body (1) A coil heat exchanger (8) for preheating the raw material gas is arranged between them, the furnace body (1) above the coil heat exchanger (8) is provided with a product gas outlet (11), and the expansion section of the furnace body (1) ( The lower part of 6) is provided with a high-pressure gas injection pipe (5), and the bottom of the semi-coke collection tank (7) is provided with a discharge port (12). The utility model has the advantages of low energy consumption, small hydrogen consumption and light dust removal load.
Description
Technical field
The utility model belongs to a kind of vapourizing furnace, is specifically related to a kind of vapourizing furnace for coal preparing natural gas.
Background technology
Along with the quickening of Urbanization in China and the raising of environmental requirement, the demand of Sweet natural gas is increased year by year.China's natural gas consumption in 2010 is 1,000 hundred million m
3, breach reaches 10,000,000,000 m
3.Estimate that the year two thousand twenty China's natural gas breach will reach 1,000 hundred million m
3.According to the energy situation of China, producing SNG technology by coal is the effective means that makes up natural gas source shortage.
Conventional coal preparing natural gas technology (also claiming two-step approach) is under high temperature (800-1500 DEG C), high pressure (2-4MPa), taking water vapour as vaporized chemical, coal is converted into synthetic gas (CO+H
2), synthetic gas obtains SNG again after methanation.This technological process is more ripe, has realized industrialization in 1880s in big plain in u.s.a factory, but its long flow path, investment is large, process thermal efficiency lower (61%).Coal direct hydrogenation vaporizing system SNG technology is under the condition of (850-1000 DEG C) and 7MPa, fine coal and hydrogen are added in vapourizing furnace simultaneously, rely on hydrogen to the pyrolysis of coal stage discharge the stabilization of free radical and gasifying stage and carbon active in semicoke react the gas that obtains being rich in methane, the tar light oil of while by-product high added value.Compared with two-step approach, this technical process is simple, cost of investment is low and the thermo-efficiency of process higher (79.6%).
Because the gasification of coal direct hydrogenation has above advantage, many R&D institutions have carried out a large amount of research work in this regard, and the core of research is the exploitation of hydrogasification Reaktionsofen.Institute of Gas Technology of the U.S. (IGT) adopts fluidized-bed gasification furnace to develop coal hydrogenation gasification Hygas technique at 1972-1980, has carried out the pilot scale test of 75t/d.The subject matter that fluidized-bed gasification exists is that hydrogasification reaction easily adhesive aggregation occurs and loses taking out of of fluidization and fine powder compared with slow, coal dust in stove.Thereby in the later stage seventies, hydrogasification technique develops to quick hydrogasification.Air flow bed is can service temperature high because having, gasification reaction moment completes, single stove throughput large and easily the special advantage such as amplifications become the main type of furnace that coal hydrogenation gasification process is researched and developed.Mainly be divided into single-cylinder type and the double-cylinder type with internal recycle for the type of furnace of coal hydrogenation entrained flow gasification at present.
U.S. Rockwell (Rockwell) company has set up the PDU device of 0.25t/h and the pilot scale air flow bed hydrogasification device of 1t/h in 1978-1986, vapourizing furnace adopts the single-cylinder type type of furnace, mainly formed by preheating chamber and vaporizer two portions, the effect of preheating chamber is that the temperature of the required hydrogen of reaction is brought up to 800-850 DEG C, ensures carrying out smoothly of hydrogasification reaction.This furnace type structure is relatively simple, is convenient to amplify and realizes industrialization, but it need to add a certain amount of oxygen in inlet gas, consumes hydrogen partial and improve the temperature of mixture, ensures the generation of hydrogasification, therefore hydrogen consumption is larger.
Osaka, Japan Gas Company in 1986 and company of Centrica have developed jointly BG-OG air flow bed coal hydrogenation gasification technique, this reactor is the double-cylinder type airflow bed gasification furnace with internal recycle, by the Rapid Circulation of air-flow, the heat that coal and hydrogen reaction discharge can make full use of in further pre-hot coal and hydrogen, thereby only need pass into a small amount of oxygen at a heater stage, in process, not aerobic gas can maintain temperature of reaction, and can easily regulate temperature of reaction by changing hydrogen preheating temperature, and then change products distribution.But in this vapourizing furnace, the circulation of a large amount of gases need to be consumed energy larger, can under technical scale, rely on momentum that gas sprays into realize required recycle ratio still needs and wants verification experimental verification, in addition, gas is higher in the gas speed of stove internal recycle, thereby a large amount of semicoke particles are by gas entrainment, in exit gas, Dust Capacity is larger, and the load of dust remove of subsequent disposal system is heavier.
Summary of the invention
The utility model is intended to solve the problem existing in above-mentioned coal hydrogenation air flow bed, provides that a kind of power consumption is low, hydrogen consumption is little, the vapourizing furnace for coal preparing natural gas that load of dust remove is light.
The utility model adopts simple in structure and is easy to the monotubular type of furnace of amplifying, and by hydrogen preheat coil is set in vapourizing furnace, has improved the temperature of the hydrogen that enters feed nozzle, has reduced the hydrogen consumption of system; At vapourizing furnace middle part, expanding reach is set, has reduced the speed of gas, reduced the fine powder amount of carrying in gas, alleviated particulate matter load separated from the gas in subsequent product gas.
The technical solution of the utility model is: a kind of vapourizing furnace for coal preparing natural gas, this vapourizing furnace is by body of heater, vaporizer, feed nozzle, semicoke collecting tank composition, it is characterized in that body of heater is divided into, in, lower three parts, upper of furnace body is divided into vertical section, body of heater middle part is divided into expanding reach, lower portion of furnace body is divided into V font semicoke collecting tank, the inwall of body of heater is equipped with refractory materials, the top of body of heater is vaporizer, feed nozzle is positioned at the top of vaporizer, between dividing, vaporizer and upper of furnace body be provided with the coil heat exchanger to unstripped gas preheating, the bottom of body of heater expanding reach is provided with high pressure gas injection tube, the bottom of semicoke collecting tank is provided with discharge gate.
The inwall of body of heater as above is equipped with refractory materials.
The feed nozzle that is arranged on vaporizer top as above is 1-4.In the time that a feed nozzle is set, feed nozzle is in vaporizer top center position, and outlet vertically downward; In the time that two feed nozzles are set, feed nozzle is symmetrical at vaporizer top, outlet downwards and with the angle α of body of heater medullary ray 30
o-60
oin scope, regulate and arrange; In the time that three feed nozzles are set, feed nozzle is uniformly distributed at vaporizer top, outlet downwards and with the angle α of body of heater medullary ray 30
o-60
oin scope, regulate and arrange; In the time that four feed nozzles are set, feed nozzle can be evenly distributed on vaporizer top, outlet downwards and with the angle α of body of heater medullary ray 30
o-60
oregulate and arrange in scope, also can be wherein three be uniformly distributed at vaporizer top, outlet downwards and with the angle α of body of heater medullary ray 30
o-60
oin scope, regulate and arrange, another is in vaporizer top center position, and outlet vertically downward.
The top of coil heat exchanger as above is provided with low temperature hydrogen entrance, and the bottom of coil heat exchanger is provided with high-temperature hydrogen outlet.
The high pressure gas injection tube that is arranged on expanding reach bottom as above is 4-6, and outlet scope downward and body of heater medullary ray angle γ is 30
o-60
o, with the scope of horizontal plane angle β be 30
o-60
o.
High pressure gas jet pipe as above high pressure gas used are nitrogen or water vapour.
The temperature of vaporizer as above is 750-900 DEG C, and after preheating, the temperature of hydrogen is 400-550 DEG C.
The vaporized chemical that enters feed nozzle as above is the gas mixture of hydrogen and a small amount of oxygen.
Working process of the present utility model is: feed coal enters vapourizing furnace through feed nozzle together with vaporized chemical (hydrogen and a small amount of oxygen), react in vaporizer generating gasification, gas product is realized and being separated in expanding reach with solid product semicoke, gas product enters the annular space space between vaporizer and body of heater, after coil heat exchanger cooling, leave vapourizing furnace from product gas outlet, solid phase semicoke falls into semicoke collecting tank, regularly utilizes high pressure gas to jet to it, discharges vapourizing furnace by discharge gate.
Major advantage of the present utility model is the vaporizer structure that has adopted straight barrel type, furnace binding is simple, in vaporizer bottom, expanding reach is set, reduce the gas speed of gas product, be conducive to separating of gas product and solid semicoke, high-temperature product gas after separating with semicoke enters the annular space space between vaporizer and body of heater through baffling, after lowering the temperature with hydrogen coil heat exchange, leave vapourizing furnace, exit gas volume reduces, reduce particulate matter drag-out in gas, simultaneously preheating enter the hydrogen of reactor, integrate reactor and waste heat boiler, improve heat utilization efficiency, reduced the load of follow-up purification process simultaneously, be conducive to cost-saving.
Brief description of the drawings
Fig. 1 is utility model vapourizing furnace longitudinal profile structural representation.
Fig. 2 is the A-A face vertical view of utility model vapourizing furnace when a nozzle is set.
Fig. 3 is the A-A face vertical view of utility model vapourizing furnace when two nozzles are set.
Fig. 4 is the A-A face vertical view of utility model vapourizing furnace when three nozzles are set.
Fig. 5, Fig. 6 are the A-A face vertical view of utility model vapourizing furnace when four nozzles are set.
Fig. 7 is utility model vapourizing furnace vapourizing furnace B-B face vertical view.
As shown in the figure: 1. body of heater; 2. vaporizer; 3. feed nozzle; 4. refractory materials; 5. high pressure gas injection tube; 6. expanding reach; 7. semicoke collecting tank; 8. raw hydrogen preheat coil; 9. high-temperature hydrogen outlet; 10. low temperature hydrogen entrance; 11. product gas outlet; 12. discharge gates.
Embodiment
Embodiment 1
A kind of vapourizing furnace for coal preparing natural gas, this vapourizing furnace is by body of heater 1, feed nozzle 3, vaporizer 2, semicoke collecting tank 7 forms, the inwall of body of heater 1 scribbles refractory materials 4, body of heater 1 is divided into, in, lower three parts, body of heater 1 top is divided into vertical section, body of heater 1 middle part is divided into expanding reach 6, body of heater 1 bottom is divided into V font semicoke collecting tank 7, body of heater 1 top is divided into vaporizer 2, 1 feed nozzle 3 is positioned at the central position on the top of vaporizer 2, outlet vertically downward, between dividing on vaporizer 2 and body of heater 1 top, be provided with the coil heat exchanger 8 to unstripped gas preheating, the top of coil heat exchanger 8 is provided with low temperature hydrogen entrance 10, the bottom of coil heat exchanger 8 is provided with high-temperature hydrogen outlet 9, the body of heater 1 of coil heat exchanger 8 tops is provided with product gas outlet 11, the bottom of body of heater 1 expanding reach 6 is provided with 4 high pressure gas injection tubes 5, outlet scope downward and body of heater 1 medullary ray angle γ is 30
o, with the scope of horizontal plane angle β be 60
o, the bottom of semicoke collecting tank 7 is provided with discharge gate 12.
Working process is: feed coal enters vapourizing furnace with together with the hydrogen vaporized chemical of 1000 DEG C through feed nozzle 3, generating gasification reaction in vaporizer 2, temperature of reaction in vapourizing furnace 2 is 850 DEG C, reacted high-temperature product gas enters in expanding reach 6 and separates with solid product semicoke, the gas product of 830 DEG C after separation enters the annular space space between vaporizer 2 and body of heater 1 top, coil heat exchanger 8, carry out heat exchange with the raw hydrogen entering from low temperature hydrogen entrance 10, make the temperature of gas product be down to 600 DEG C, gas product after cooling leaves vapourizing furnace from product gas outlet 11, enter follow-up purification section, solid phase semicoke falls into semicoke collecting tank 7, regularly utilize high pressure nitrogen or water vapour to spray into from high pressure gas injection tube 5, solid phase semicoke is discharged to vapourizing furnace through discharge gate 12.Raw hydrogen through in coil heat exchanger 8 with the heat exchange of high-temperature product gas after, temperature rises to 500 DEG C, from leaving, high-temperature hydrogen outlet 9 enters feed nozzle 3, in feed nozzle 3, react with a small amount of oxygen generation perfect combustion, consume hydrogen partial remaining hydrogen is further warming up to 1000 DEG C, enter together with feed coal afterwards and in vaporizer 2, carry out hydrogasification reaction.
Embodiment 2
3 feed nozzles 3 are positioned at being uniformly distributed of top of vaporizer 2, outlet downwards and with the angle α of body of heater 1 medullary ray 60
oin scope, regulate and arrange, the bottom of body of heater 1 expanding reach 6 is provided with 5 high pressure gas injection tubes 5, and outlet scope downward and body of heater 1 medullary ray angle γ is 45
o, with the scope of horizontal plane angle β be 45
o.All the other are with embodiment 1.
Embodiment 3
4 feed nozzles 3, wherein three are uniformly distributed at vaporizer 2 tops, outlet downwards and with the angle α of body of heater 1 medullary ray 30
oin scope, regulate and arrange, another is in vaporizer 2 top center positions, and outlet vertically downward.The bottom of body of heater 1 expanding reach 6 is provided with 6 high pressure gas injection tubes 5, and outlet scope downward and body of heater 1 medullary ray angle γ is 60
o, with the scope of horizontal plane angle β be 30
o.All the other are with embodiment 1.
Claims (8)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320731815.8U CN203700291U (en) | 2013-11-19 | 2013-11-19 | Gasification furnace for synthetic natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320731815.8U CN203700291U (en) | 2013-11-19 | 2013-11-19 | Gasification furnace for synthetic natural gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203700291U true CN203700291U (en) | 2014-07-09 |
Family
ID=51050757
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201320731815.8U Expired - Lifetime CN203700291U (en) | 2013-11-19 | 2013-11-19 | Gasification furnace for synthetic natural gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203700291U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104498075A (en) * | 2014-12-19 | 2015-04-08 | 中美新能源技术研发（山西）有限公司 | Quick hydropyrolysis reactor and process thereof |
| CN104946292A (en) * | 2015-06-08 | 2015-09-30 | 中美新能源技术研发（山西）有限公司 | Novel reactor for making oil through powdered coal hydropyrolysis and technology |
-
2013
- 2013-11-19 CN CN201320731815.8U patent/CN203700291U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104498075A (en) * | 2014-12-19 | 2015-04-08 | 中美新能源技术研发（山西）有限公司 | Quick hydropyrolysis reactor and process thereof |
| CN104946292A (en) * | 2015-06-08 | 2015-09-30 | 中美新能源技术研发（山西）有限公司 | Novel reactor for making oil through powdered coal hydropyrolysis and technology |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20140709 |