CN204824751U - Ft synthesis oil and coal tar is process units of hydrogenation production national standard oil altogether - Google Patents
Ft synthesis oil and coal tar is process units of hydrogenation production national standard oil altogether Download PDFInfo
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- CN204824751U CN204824751U CN201520492708.3U CN201520492708U CN204824751U CN 204824751 U CN204824751 U CN 204824751U CN 201520492708 U CN201520492708 U CN 201520492708U CN 204824751 U CN204824751 U CN 204824751U
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Abstract
The utility model discloses a ft synthesis oil and coal tar is process units of hydrogenation production national standard oil altogether, including blend stock supply of oil device, the heating furnace that goes into operation, reactor and high -pressure heat exchanger, blend stock supply of oil device export link to each other with the heating furnace feed inlet that goes into operation, the heating furnace that goes into operation export links to each other with the entry of reactor, the gas exports of reactor links to each other with an import of high -pressure heat exchanger, another entry of high -pressure heat exchanger lets in hydrogen, an export of high -pressure heat exchanger links to each other with the separates on cooling device through the pipeline that has the desalinized water entry, another export links to each other with the feed inlet of the heating furnace that goes into operation, the result oil of the liquid phase export discharge after -separating of reactor. This ft synthesis oil and coal tar is process units of hydrogenation production national standard oil altogether has a conversion per pass height, and process flow is short, and high -tension apparatus is small in quantity, and the investment cost is economized, and the running cost is low, and product quality is good, safe and reliable's characteristics.
Description
Technical field
The utility model belongs to coal chemical technology, is specifically related to the process unit of a kind of Fischer-Tropsch synthesis oil and the common hydrogenation production GB oil of coal tar.
Background technology
Along with Chinese national economy develops rapidly, increasing to the demand of processed oil, and China's income of residents steady-state growth, standard of living improves constantly, Oil Products Consumption is made still to be in a stage comparatively fast increased, but China's oil resource scarcity, becomes the important restriction factor of China's Economic development.In order to ensure national energy security and sustainable economic development, China's coal liquifaction product has had fast development nearly ten years.In addition, the urban air pollution of China just by coal fire discharged, develop to vehicular emission and compound pollution.In recent years, large-scale haze phenomenon causes the common people's giving more sustained attention air pollution problems inherent.Wherein, vehicular emission plays more crucial effect to whole air-polluting impact, and oil quality problem is one of important factor polluted.Meanwhile, China formally implements derv fuel oil IV stage criterion, and future is progressively transitioned into the V stage.
DCL/Direct coal liquefaction, ICL for Indirect Coal Liquefaction (F-T synthesis) and coal tar hydrogenating lighting are three large technology of coal liquifaction.In the production technique of existing coal tar hydrogenating lighting, produce diesel oil distillate cetane value be only 37 ~ 43, " GB19147-2013 derv fuel oil (IV) " standard-required cannot be reached.Synthetic oil (intermediate product) density that ICL for Indirect Coal Liquefaction (F-T synthesis) is produced reaches 0.81gcm-3, but product diesel oil density only about the 0.76gcm-3 after further hydrotreatment, does not still reach existing " GB19147-2013 derv fuel oil (IV) " standard.The sale of finished goods channel that China is formal can not be entered, can only be in harmonious proportion to form as processed oil and divide, there is market price low, the shortcoming that profit margin is little.And the hydrotreater of existing Fischer-Tropsch synthesis oil and hydrogenation of tar lighting device, all have employed traditional refining of petroleum hydrogenation technique, specific aim is not had to Fischer-Tropsch synthesis oil and coal tar component characteristic, cause the diesel oil of production can not (GB1947-2013IV) completely up to standard, per pass conversion is low, and diesel yield is low, and reaction generates the heavy distillate iterative cycles in oil, finally cause systemic resistance to go up very fast, often the cycle of operation only has 7000 hours continuously.And coal tar does not have the heavy bitumen matter of complete reaction to separate out in colloidal in process of cooling in hydrogenation process, be attached on pipeline and heat-exchange equipment internal surface, the resistance of ducting is caused to fall greatly, heat-exchange equipment weak effect, even also cause key instrument malfunction in hydrogenation technique device, directly threaten the safe and stable operation of hydrogenation technique device.
Utility model content
In order to make up the deficiencies in the prior art, the utility model proposes the process unit of a kind of Fischer-Tropsch synthesis oil and the common hydrogenation production GB oil of coal tar.
The utility model is achieved through the following technical solutions:
A kind of Fischer-Tropsch synthesis oil and coal tar are total to the process unit of hydrogenation production GB oil, comprise mixing raw material supply of oil device, go into operation process furnace, reactor and high pressure heat exchanger, described mixing raw material supply of oil device outlet is connected with the process furnace feed(raw material)inlet that goes into operation, the furnace outlet that goes into operation is connected with the entrance of reactor, the gaseous phase outlet of reactor is connected with high pressure heat exchanger import, another entrance of high pressure heat exchanger passes into hydrogen, an outlet of high pressure heat exchanger is connected with refrigerated separation device through the pipeline with de-salted water entrance, another outlet is connected with the feed(raw material)inlet of the process furnace that goes into operation, the liquid-phase outlet of reactor discharges the product oil after being separated.
Described reactor comprises lighting reactor and reforming reactor; The outlet of the described process furnace that goes into operation is connected with the top entry of lighting reactor, the outlet at bottom of lighting reactor is connected with the top entry of reforming reactor, reforming reactor segregation section sidepiece gaseous phase outlet is connected with an import of high pressure heat exchanger, the product oil after being separated is discharged in the outlet of reforming reactor segregation section bottom liquid phases, an outlet of high pressure heat exchanger is connected with refrigerated separation device through the pipeline with de-salted water entrance, another entrance of high pressure heat exchanger passes into hydrogen, and another outlet is connected with the feed(raw material)inlet of the process furnace that goes into operation.
Described refrigerated separation device comprises air-conditioning water cooler, high-pressure separator and circulating hydrogen compressor, an outlet of high pressure heat exchanger is connected with air-conditioning water cooler entrance through the pipeline with de-salted water entrance, air-conditioning cooler outlet is connected with high-pressure separator entrance, the top gas outlet point two-way of high-pressure separator, one tunnel is directly discharged, one tunnel is connected with circulating hydrogen suction port of compressor, circulating hydrogen compressor outlet divides two-way, one tunnel is connected with reforming reactor top entry, one tunnel is connected with high pressure heat exchanger entrance through the pipeline with hydrogen inlet, the product oil that the bottom liquid phases oil of high-pressure separator is separated with reforming reactor segregation section is sent by after line-blending, bottom high-pressure separator, sewage outlet is connected with sewage device.
The aspect ratio of lighting reactor is 6 ~ 15, and lighting reactor catalyst bed individual layer height is the lighting reactor diameter of 2 ~ 3.5 times.
The aspect ratio of described lighting reactor is 8 ~ 12, and lighting reactor catalyst bed individual layer height is the lighting reactor diameter of 2 ~ 2.8 times.
Reforming reactor is made up of two portions, upper part is conversion zone, and bottom is divided into segregation section, and the aspect ratio of reforming reactor is 5 ~ 14, conversion zone and segregation section aspect ratio are 3 ~ 4.5, and reforming reactor beds individual layer height is the reforming reactor diameter of 0.7 ~ 1 times.
The aspect ratio of reforming reactor is 7 ~ 10, and conversion zone and segregation section aspect ratio are 3.2 ~ 4, and reforming reactor beds individual layer height is the reforming reactor diameter of 0.7 ~ 0.8 times.
Described mixing raw material supply of oil device comprises mixing tank, stock oil well heater and raw oil pump, described mixing tank is provided with F-T synthesis oil-in and coal tar entrance, mixing tank outlet is connected with stock oil calorifier inlets, stock oil heater outlet is connected with raw oil pump entrance, and raw oil pump outlet is connected with the process furnace feed(raw material)inlet that goes into operation.
Stock oil well heater is tube and shell heat exchanger.
The process furnace that goes into operation is lying pipe list radiation furnace, and high pressure heat exchanger is the U-shaped tubular heat exchanger of diaphragm seal formula.
Compared with prior art, the utility model has following useful technique effect:
The Fischer-Tropsch synthesis oil that the utility model provides and coal tar are total to the process unit of hydrogenation production GB oil, and have per pass conversion high, technical process is short, and high-tension apparatus quantity is few, and investment cost is economized, and running cost is low, good product quality, safe and reliable feature.
Accompanying drawing explanation
Fig. 1 is process unit structural representation of the present utility model, wherein sequence number 1 is mixing tank, 2 is stock oil well heater, 3 is raw oil pump, 4 is the process furnace that goes into operation, 5 is lighting reactor, 6 is reforming reactor, 7 is high pressure heat exchanger, 8 is air-conditioning water cooler, 9 is high-pressure separator, 10 is circulating hydrogen compressor, 11 is high pressure Separation of Water reducing valve, 12 is high pressure separating oil reducing valve, 13 for generating oily reducing valve, 14 is mixing hydrogen control valve, a is Fischer-Tropsch synthesis oil, b is coal tar, c is discharge hydrogen, d is pure hydrogen, e is de-salted water, f is that sulfur-bearing contains ammonia sewage, g is product oil.
Embodiment
Below in conjunction with specific embodiment, the utility model is described in further detail, described in be to explanation of the present utility model instead of restriction.
See Fig. 1, a kind of Fischer-Tropsch synthesis oil and coal tar are total to the process unit of hydrogenation production GB oil, comprise vertical mixing tank 1, stock oil well heater 2, raw oil pump 3, go into operation process furnace 4, lighting reactor 5, reforming reactor 6, high pressure heat exchanger 7, air-conditioning water cooler 8, high-pressure separator 9, circulating hydrogen compressor 10 and valve, described mixing tank 1 is provided with Fischer-Tropsch synthesis oil a entrance and coal tar b entrance, mixing tank 1 exports and is connected with stock oil well heater 2 entrance, stock oil well heater 2 exports and is connected with raw oil pump 3 entrance, raw oil pump 3 exports and is connected with process furnace 4 feed(raw material)inlet that goes into operation, the outlet of the described process furnace 4 that goes into operation is connected with the top entry of lighting reactor 5, the outlet at bottom of lighting reactor 5 is connected with the top entry of reforming reactor 6, reforming reactor 6 segregation section sidepiece gaseous phase outlet is connected with an import of high pressure heat exchanger 7, the product oil after being separated is discharged in the outlet of reforming reactor 6 segregation section bottom liquid phases, an outlet of high pressure heat exchanger 7 is connected with air-conditioning water cooler 8 entrance through the pipeline with de-salted water e entrance, air-conditioning water cooler 8 exports and is connected with high-pressure separator 9 entrance, the top gas outlet point two-way of high-pressure separator 9, one tunnel is directly discharged, one tunnel is connected with circulating hydrogen compressor 10 entrance, circulating hydrogen compressor 10 exports a point two-way, one tunnel is connected with reforming reactor 6 top entry, one tunnel is connected with high pressure heat exchanger 7 entrance through the pipeline with hydrogen inlet, another outlet of high pressure heat exchanger 7 is connected with the feed(raw material)inlet of the process furnace 4 that goes into operation, the product oil that the bottom liquid phases oil of high-pressure separator 9 is separated with reforming reactor 6 segregation section is sent by after line-blending, bottom high-pressure separator 9, sewage outlet is connected with sewage device.
Wherein, the aspect ratio of lighting reactor 5 is 6 ~ 15, and lighting reactor 5 beds individual layer height is the lighting reactor diameter of 2 ~ 3.5 times; Preferably, the aspect ratio of described lighting reactor 5 is 8 ~ 12, and lighting reactor 5 beds individual layer height is the lighting reactor diameter of 2 ~ 2.8 times.Stock oil well heater 2 is tube and shell heat exchanger; Go into operation process furnace 4 for lying pipe list radiation furnace, and high pressure heat exchanger 7 is the U-shaped tubular heat exchanger of diaphragm seal formula.
Further, reforming reactor 6 is made up of two portions, and upper part is conversion zone, bottom is divided into segregation section, the aspect ratio of reforming reactor 6 is 5 ~ 14, and conversion zone and segregation section aspect ratio are 3 ~ 4.5, and reforming reactor beds individual layer height is the reforming reactor diameter of 0.7 ~ 1 times.Preferably, the aspect ratio of reforming reactor 6 is 7 ~ 10, and conversion zone and segregation section aspect ratio are 3.2 ~ 4, and reforming reactor beds individual layer height is the reforming reactor diameter of 0.7 ~ 0.8 times.
It should be noted that, the pipeline that high pressure heat exchanger 7 is connected with process furnace 4 feed(raw material)inlet that goes into operation is provided with and mixes hydrogen control valve 14, the bottom liquid phases oil export pipeline of high-pressure separator 9 is provided with high pressure separating oil reducing valve 12, and bottom high-pressure separator 9, sewage outlet Outer Tube is provided with high pressure Separation of Water reducing valve 11; Reforming reactor 6 segregation section bottom liquid phases outlet conduit is provided with and generates oily reducing valve 13.
Principle of work of the present utility model:
Fischer-Tropsch synthesis oil and coal tar are sent into respectively in vertical mixing tank through pipeline and are mixed, and mixed mixing oil is from the incoming stock oil heater of mixing tank outlet at bottom.After mixing oil heat temperature raising in stock oil well heater, boosted by raw oil pump.Raw oil pump exports after the high pressure mixing oil sent mixes with the mixed hydrogen from high pressure heat exchanger and enters and go into operation in the boiler tube of process furnace.During normal running, process furnace is in cold stoking state.From going into operation, process furnace mixed hydrogen oil out enters from lighting reactor head, carries out the lighting process of mixing oil.The product oil that bottom is discharged is delivered to after reforming reactor top mixes with hydrogen through pipeline and is entered reforming reactor.The reaction product completing reaction at conversion zone falls to segregation section and carries out gas-liquid two-phase separation.Discharged from the isolated gas-phase product of reforming reactor segregation section by reforming reactor segregation section lateral outlet, after pipeline feeding high pressure heat exchanger is lowered the temperature.Gas-phase product after high pressure heat exchanger heat exchange cooling to mix with de-salted water to send into be sent into high-pressure separator after its temperature is down to 40 ~ 45 DEG C by air-conditioning water cooler and again carries out Oil, Water, Gas three phase separation, gas phase after separation uses through recycle gas compressor boosting Posterior circle, the product oil that liquid phase oil is separated with reforming reactor segregation section, by carrying device after line-blending, is separated the aqueous phase obtained and send sewage device.
Being rich in a large amount of bituminous matters and colloid in the middle of well-known coal tar, is the key of its hydrogenation lighting process.The basic structure of bituminous matter and colloid be the aromatic ring condensed that forms with multiple aromatic nucleus for core, be connected with several naphthenic hydrocarbon around.The positive structure that aromatic nucleus and naphthenic hydrocarbon also differ with several length or the alkyl group side chain of isomery, be also mingled with the gene of sulphur, oxygen, nitrogen in molecule, also complexing has the metal such as nickel, vanadium iron simultaneously.Just easily there is heat scission reaction after being heated and generate charcoal, be deposited in catalyst surface micropore, affect catalyst activity and add reactor beds layer resistance.And hydrogen solubleness in alkane is greater than the solubleness in aromatic hydrocarbons, the solubleness of hydrogen in alkane increases with carbon number (relative molecular mass) and increases, and the solubleness of hydrogen in aromatic hydrocarbons increasing and reduce with aromatic hydrocarbons number of rings, the solubleness of hydrogen in non-hydrocarbons sulfur-bearing and organic compounds containing nitrogen is but starkly lower than the solubleness in hydro carbons.Fischer-Tropsch synthesis oil (Low Temperature Fischer Tropsch synthetic oil) is not containing non-hydrocarbons sulfur-bearing and organic compounds containing nitrogen, and aliphatic hydrocarbons a large amount of in having, and is conducive to the dispersion of hydrogen in stock oil and dissolving.And hydrogen dissolves dispersion and effectively prevents the raw charcoal reaction of bituminous matter condensation in the middle of stock oil, extend the process unit cycle of operation.Simultaneously, the process generating heavy bitumen matter due to the fracture of bituminous matter hydrogenation process generation side chain is unavoidable, therefore process unit of the present utility model eliminates the reaction generation oil cooling apparatus of prior art, being dissolved in reaction at high operating temperatures by not having the heavy bitumen matter of complete reaction generates in oil, make it take follow-up low-pressure distillation systematic position to remove, there is the feature of the simple and easy row of method.
The utility model heats under also carrying out low pressure operating mode to Hydrogenation raw oil, reduces high temperature service and drops into, simplify technical process, reduce hydrogenation technique equipment safety risk.Fischer-Tropsch synthesis oil (Low Temperature Fischer Tropsch synthetic oil) after process unit process of the present utility model, still remains higher cetane value.Coal tar (middle coalite tar or coal-tar heavy oil) simultaneously after process unit process of the present utility model, maintain the low-sulfur oilness of diesel oil, also reduce the total thrcylic aromatic hydrocarbon content in the middle of its diesel oil in polycyclic aromatic hydrocarbons component, the discharge of particulate matter (PM) and NOx when effectively reducing diesel combustion.
The Fischer-Tropsch synthesis oil that the utility model provides and coal tar are total to the process unit of hydrogenation production GB oil, have employed Fischer-Tropsch synthesis oil (Low Temperature Fischer Tropsch synthetic oil) and coal tar (middle coalite tar or coal-tar heavy oil) charge proportion is that between 0.1 ~ 10, common mixed hydrogenation all can produce qualified GB (GB19147-2013IV) diesel oil, it is high that this device has per pass conversion, technical process is short, high-tension apparatus quantity is few, investment cost is economized, running cost is low, good product quality, safe and reliable feature.
More than show and describe ultimate principle of the present utility model and principal character and advantage of the present utility model.The technician of the industry should understand; the utility model is not restricted to the described embodiments; what describe in above-described embodiment and specification sheets just illustrates principle of the present utility model; under the prerequisite not departing from the utility model spirit and scope; the utility model also has various changes and modifications, and these changes and improvements all fall within the scope of claimed the utility model.The claimed scope of the utility model is defined by appending claims and equivalent thereof.
Claims (10)
1. a Fischer-Tropsch synthesis oil and coal tar are total to the process unit of hydrogenation production GB oil, it is characterized in that, comprise mixing raw material supply of oil device, go into operation process furnace (4), reactor and high pressure heat exchanger (7), described mixing raw material supply of oil device outlet is connected with the process furnace that goes into operation (4) feed(raw material)inlet, the process furnace (4) that goes into operation outlet is connected with the entrance of reactor, the gaseous phase outlet of reactor is connected with an import of high pressure heat exchanger (7), another entrance of high pressure heat exchanger (7) passes into hydrogen, an outlet of high pressure heat exchanger (7) is connected with refrigerated separation device through the pipeline with de-salted water (e) entrance, another outlet is connected with the feed(raw material)inlet of the process furnace that goes into operation (4), the liquid-phase outlet of reactor discharges the product oil after being separated.
2. Fischer-Tropsch synthesis oil according to claim 1 and coal tar are total to the process unit of hydrogenation production GB oil, and it is characterized in that, described reactor comprises lighting reactor (5) and reforming reactor (6), the outlet of the described process furnace that goes into operation (4) is connected with the top entry of lighting reactor (5), the outlet at bottom of lighting reactor (5) is connected with the top entry of reforming reactor (6), reforming reactor (6) segregation section sidepiece gaseous phase outlet is connected with an import of high pressure heat exchanger (7), the product oil after being separated is discharged in the outlet of reforming reactor (6) segregation section bottom liquid phases, an outlet of high pressure heat exchanger (7) is connected with refrigerated separation device through the pipeline with de-salted water (e) entrance, another entrance of high pressure heat exchanger (7) passes into hydrogen, another outlet is connected with the feed(raw material)inlet of the process furnace that goes into operation (4).
3. Fischer-Tropsch synthesis oil according to claim 2 and coal tar are total to the process unit of hydrogenation production GB oil, it is characterized in that, described refrigerated separation device comprises air-conditioning water cooler (8), high-pressure separator (9) and circulating hydrogen compressor (10), an outlet of high pressure heat exchanger (7) is connected with air-conditioning water cooler (8) entrance through the pipeline with de-salted water (e) entrance, air-conditioning water cooler (8) outlet is connected with high-pressure separator (9) entrance, the top gas outlet point two-way of high-pressure separator (9), one tunnel is directly discharged, one tunnel is connected with circulating hydrogen compressor (10) entrance, circulating hydrogen compressor (10) outlet point two-way, one tunnel is connected with reforming reactor (6) top entry, one tunnel is connected with high pressure heat exchanger (7) entrance through the pipeline with hydrogen inlet, the product oil that the bottom liquid phases oil of high-pressure separator (9) is separated with reforming reactor segregation section is sent by after line-blending, high-pressure separator (9) bottom sewage outlet is connected with sewage device.
4. Fischer-Tropsch synthesis oil according to claim 2 and coal tar are total to the process unit of hydrogenation production GB oil, it is characterized in that, the aspect ratio of lighting reactor (5) is 6 ~ 15, and lighting reactor (5) beds individual layer height is the lighting reactor diameter of 2 ~ 3.5 times.
5. Fischer-Tropsch synthesis oil according to claim 4 and coal tar are total to the process unit of hydrogenation production GB oil, it is characterized in that, the aspect ratio of described lighting reactor (5) is 8 ~ 12, and lighting reactor (5) beds individual layer height is the lighting reactor diameter of 2 ~ 2.8 times.
6. Fischer-Tropsch synthesis oil according to claim 2 and coal tar are total to the process unit of hydrogenation production GB oil, it is characterized in that, reforming reactor (6) is made up of two portions, upper part is conversion zone, bottom is divided into segregation section, the aspect ratio of reforming reactor (6) is 5 ~ 14, and conversion zone and segregation section aspect ratio are 3 ~ 4.5, and reforming reactor beds individual layer height is the reforming reactor diameter of 0.7 ~ 1 times.
7. Fischer-Tropsch synthesis oil according to claim 6 and coal tar are total to the process unit of hydrogenation production GB oil, it is characterized in that, the aspect ratio of reforming reactor (6) is 7 ~ 10, conversion zone and segregation section aspect ratio are 3.2 ~ 4, and reforming reactor beds individual layer height is the reforming reactor diameter of 0.7 ~ 0.8 times.
8. Fischer-Tropsch synthesis oil according to claim 1 and coal tar are total to the process unit of hydrogenation production GB oil, it is characterized in that, described mixing raw material supply of oil device comprises mixing tank (1), stock oil well heater (2) and raw oil pump (3), described mixing tank (1) is provided with Fischer-Tropsch synthesis oil (a) entrance and coal tar (b) entrance, mixing tank (1) outlet is connected with stock oil well heater (2) entrance, stock oil well heater (2) outlet is connected with raw oil pump (3) entrance, raw oil pump (3) exports and is connected with the process furnace that goes into operation (4) feed(raw material)inlet.
9. Fischer-Tropsch synthesis oil according to claim 7 and coal tar are total to the process unit of hydrogenation production GB oil, and it is characterized in that, stock oil well heater (2) is tube and shell heat exchanger.
10. Fischer-Tropsch synthesis oil according to claim 1 and coal tar are total to the process unit of hydrogenation production GB oil, it is characterized in that, go into operation process furnace (4) for lying pipe list radiation furnace, and high pressure heat exchanger (7) is the U-shaped tubular heat exchanger of diaphragm seal formula.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201520492708.3U CN204824751U (en) | 2015-07-09 | 2015-07-09 | Ft synthesis oil and coal tar is process units of hydrogenation production national standard oil altogether |
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| CN201520492708.3U CN204824751U (en) | 2015-07-09 | 2015-07-09 | Ft synthesis oil and coal tar is process units of hydrogenation production national standard oil altogether |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104987885A (en) * | 2015-07-09 | 2015-10-21 | 陕西美斯林能源科技研究院 | Technology and device for producing national standard oil through fischer-tropsch synthesis oil and coal tar through hydrogenation |
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2015
- 2015-07-09 CN CN201520492708.3U patent/CN204824751U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104987885A (en) * | 2015-07-09 | 2015-10-21 | 陕西美斯林能源科技研究院 | Technology and device for producing national standard oil through fischer-tropsch synthesis oil and coal tar through hydrogenation |
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Granted publication date: 20151202 Termination date: 20180709 |