CN205061981U - Coke oven gas directly produces fuel oil device - Google Patents
Coke oven gas directly produces fuel oil device Download PDFInfo
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- CN205061981U CN205061981U CN201520709433.4U CN201520709433U CN205061981U CN 205061981 U CN205061981 U CN 205061981U CN 201520709433 U CN201520709433 U CN 201520709433U CN 205061981 U CN205061981 U CN 205061981U
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- Prior art keywords
- compressor
- pretreater
- gas
- psa
- coke
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Abstract
The utility model discloses a coke oven gas directly produces fuel oil device, including the desulfurizing tower, a compressor, hydrogenation ware in advance, the hydrogenation ware, reborner and ft synthesis reactor, the desulfurizing tower is connected in the single -stage -compression import of compressor, TSA pretreater and PSA pretreater has connected gradually in the single -stage -compression export of compressor, the exit linkage of PSA pretreater is in the second grade compression import of compressor, hydrogenation ware in advance connects gradually in the second grade compression export of compressor, the hydrogenation ware, the flue gas desulfurization reaction ware, the reborner, adsorption tower and ft synthesis reactor, the gas outlet connection on adsorption tower top is on the air inlet on the top of reborner. The utility model discloses the device flow is simple, easily operation, and stable operation for a long time can effectively reduce energy consumption and equipment investment, realizes energy -concerving and environment -protective purpose.
Description
Technical field
The utility model relates to coke-oven gas technical field of comprehensive utilization, specifically a kind of coke-oven gas direct production oil fuel device.
Background technology
China is the country that world's coke output is maximum, accounts for 60% of global coke output, and often produces one ton of coke and will to have an appointment 400Nm
3byproduct coke-oven gas produce, output is huge, becomes a kind of large-tonnage energy and chemical resource gradually.
Coke-oven gas is also known as coke(oven)gas, its composition is slightly difference because coking coal quality is different with coking condition, generally contain the hydrogen of about 55%, the methane of about 25%, the carbon monoxide of about 7%, also contains the nitrogen of about 5%, the unsaturated hydrocarbons of about 3% in addition, the carbonic acid gas of about 2%, the oxygen of about 1% and other gas.Traditional treatment process is extremely limited, mainly be used as the heating of coke-oven gas self, town gas and generating, and due to the defect for the treatment of unit, make existing treatment unit processing efficiency low, cost is high, and therefore in the consideration of safety in production, coke-oven gas more than needed is then directly discharged in air after burning, not only pollute environment but also cause great waste, bring great threat also to the living environment of the mankind.Therefore, how efficiently, reasonably utilize coke-oven gas to be the key subjects of relation environmental protection, comprehensive utilization of resources, energy-saving and emission-reduction, between nearest decades, obtained everybody showing great attention to.Owing to containing a large amount of hydrocarbon resources in coke-oven gas, a lot of method about its comprehensive utilization and device are therefore there is so far.
Utility model content
The purpose of this utility model is to provide a kind of coke-oven gas direct production oil fuel device, to solve the problem proposed in above-mentioned background technology.
For achieving the above object, the utility model provides following technical scheme:
A kind of coke-oven gas direct production oil fuel device, comprise thionizer, compressor, pre-hydrogenator, hydrogenator, converter and Fischer-Tropsch synthesis device, described thionizer is connected in the one stage of compression import of compressor, the one stage of compression outlet of compressor is connected with TSA pretreater and PSA pretreater in turn, the outlet of PSA pretreater is connected in the two-stage compression import of compressor, the two-stage compression outlet of compressor connects pre-hydrogenator successively, hydrogenator, desulphurization reactor, converter, adsorption tower and Fischer-Tropsch synthesis device, the air outlet on described adsorption tower top is connected on the inlet mouth on the top of converter.
As the further scheme of the utility model: the gas feed on described converter top is also connected with middle pressure steam inlet pipe.
As the utility model further scheme again: described TSA pretreater and PSA pretreater are equipped with two.
Compared with prior art, the beneficial effects of the utility model are:
1) the utility model device flow process is simple, easy handling, the operation of energy long-time stable, and processing efficiency is high, and cost is low;
2) the utility model device effectively utilizes carbon, the hydrogen resource in coke-oven gas, and whole production process only needs supplementary part water vapour for methane conversion, decreases energy expenditure and facility investment; Meanwhile, the recycle of carbon dioxide gas physical efficiency, reduces the discharge of carbonic acid gas to a certain extent, realizes the object of energy-conserving and environment-protective;
3) only just can directly need be sold as qualified product through simple rectifying by the utility model device, the production for oil fuel provides a new approach.
Accompanying drawing explanation
Fig. 1 is flow path device figure of the present utility model.
Fig. 2 is the workflow sketch of the utility model device.
In figure: 1-thionizer; 2-compressor; 3-TSA pretreater; 4-PSA pretreater; 5-pre-hydrogenator; 6-hydrogenator; 7-desulphurization reactor; 8-converter; 9-adsorption tower; 10-Fischer-Tropsch synthesis device.
Embodiment
Below in conjunction with the accompanying drawing in the utility model embodiment, be clearly and completely described the technical scheme in the utility model embodiment, obviously, described embodiment is only the utility model part embodiment, instead of whole embodiments.Based on the embodiment in the utility model, those of ordinary skill in the art are not making the every other embodiment obtained under creative work prerequisite, all belong to the scope of the utility model protection.
Refer to Fig. 1, a kind of coke-oven gas direct production oil fuel device, comprise thionizer 1, compressor 2, pre-hydrogenator 5, hydrogenator 6, converter 8 and Fischer-Tropsch synthesis device 10, thionizer 1 is connected in the one stage of compression import of compressor 2, the one stage of compression outlet of compressor 2 is connected with TSA pretreater 3 and PSA pretreater 4 in turn, the outlet of PSA pretreater 4 is connected in the two-stage compression import of compressor 2, the two-stage compression outlet of compressor 2 connects pre-hydrogenator 5 successively, hydrogenator 6, desulphurization reactor 7, converter 8, adsorption tower 9 and Fischer-Tropsch synthesis device 10, the gas feed on converter 8 top is also connected with middle pressure steam inlet pipe, the air outlet on adsorption tower 9 top is connected on the inlet mouth on the top of converter 8.
As shown in Figures 1 and 2, the production work flow process of the utility model device.
Coke-oven gas enters thionizer 1 from tower top, and desulfurization adopts fixed bed desulfurization by dry method, the new and effective iron oxide solid desulfurating agent that ambient temperature desulfuration agent is is main active component with active iron oxide compound.Filling West China company exploitation HX-Z series solid desulfurating agent in thionizer.This sweetening agent has very high desulphurizing activated and Sulfur capacity, wherein has desulphurizing activated main component to be at normal temperatures: α-Fe
2o
3h
2o and γ-Fe
2o
3h
2o, when coal gas is by bed, the hydrogen sulfide in coal gas and desulfurization agent react and generate iron sulphide: Fe
2o
3h
2o+3H
2s=Fe
2s
3h
2o+3H
2o.
Under having oxygen existent condition in coal gas, the iron sulphide of generation generates ferric oxide with oxygen reaction again and separates out sulphur.Reaction is: Fe
2s
3h
2o+3/2O
2=Fe
2o
3h
2o+3S.As the O in coal gas
2/ H
2during S>=3, this desulfurization----regenerative process will constantly be carried out, until sweetening agent space is blocked and lost efficacy.In the process, in fact the activated iron oxide hydrate solid desulfurating agent of tool is equivalent to the effect of catalyzer.The inorganic sulfur of the overwhelming majority and a small amount of organosulfur are desulfurized the removing of agent reactive absorption, and the coke-oven gas after desulfurization and tar is sent to lower operation.
Enter after coke oven gas compressor 2 one sections is pressurized to about 0.16MPa (G) from the coke-oven gas after the desulfurization of coke oven gas desulfurization tower and enter TSA pretreater 3, PSA pretreater 4, component and most of H such as naphthalene, benzene, tar that removing is wherein remaining
2s, HCN, NH
3, the impurity composition such as hydro carbons.Pretreated coke-oven gas delivers to hydrogenating desulfurization unit below after two, three sections, compressor is compressed to about 1.6MPa (G).
Be about the gas mixture of 0.16MPa (G) from pressure after coke oven gas compressor 2 one stage of compression, enter Temp .-changing adsorption pretreater 3 from bottom, wherein one is in absorption de-oiling, naphthalene, de-benzene state, and one is in reproduced state.The regenerative process of TSA pretreater comprises: a) inverse put pressure reduction, and pretreater, against absorption direction, namely towards inlet end pressure release to resurgent gases house steward, is sent to outside battery limit (BL); B) thermal regeneration process, the stripping gas come with the regeneration of PSA pretreater, after TSA heater heats, rinses regeneration TSA pretreater, until whole bed is heated to about 120-160 DEG C, till the impurity desorptions such as the benzene in bed, naphthalene, ammonia, alkene are clean; C) process of cooling, with PSA pretreater stripping gas from birth again, cools the bed after thermal regeneration, until be cooled to normal temperature; D) boost process, against absorption direction, TSA pretreater is slowly boosted to adsorptive pressure with the purification coal gas pretreated through TSA, this pretreater just proceeds to adsorption process next time afterwards, two TSA pretreaters hocket above absorption and regenerative process, just can realize the continuous purification of gas.
Gas after Temp .-changing adsorption process is sent to PSA pretreater 4, removes the impurity composition in unstripped gas further, obtains the unstripped gas-purification coal gas of primary purification.PSA pretreater wherein also adopts a mode of operation of adsorbing a regeneration.The regenerative process of PSA pretreater comprises: a) inverse put pressure reduction, and PSA pretreater is against absorption direction, and namely towards inlet end pressure release, expellant gas is as the pretreated resurgent gases of TSA; B) rinsing desorption impurity, with the coke-oven gas after purification, rinses adsorption layer for a long time against absorption direction, makes the impurity composition of absorption be able to desorption, rinse stripping gas and be sent to TSA pre-treatment as resurgent gases; C) boost process, against absorption direction, PSA pretreater is forced into adsorptive pressure with the pretreated purification coal gas of PSA, this pretreater just proceeds to adsorption process next time.
Two PSA pretreaters hocket above absorption and regenerative process, just can realize the continuous purification of gas.
Coke-oven gas after being cleaned is sent to compressor and carries out two, three sections of compressions, enters hydrogenating desulfurization unit after pressure-raising to about 1.6MPa.
After compression, coke-oven gas enters about coke-oven gas oil removing pot removes oily post-heating to 220 ~ 300 DEG C of the trace in gas, enter pre-hydrogenator 5, oxygen here in coal gas, organosulfur, alkene etc. and hydrogen generation hydrogenation reaction, organosulfur becomes inorganic sulfur.
Reacted unstripped gas enters hydrogenator 6 after cooling, and here organosulfur will continue to carry out hydrogenation reaction with hydrogen.
Enter zinc oxide desulfurization reactor 7 dechlorination section from hydrogenator 6 synthetic gas out and remove chlorine raw material, finally enter zinc oxide desulfurization section, at this zinc oxide and hydrogen sulfide generation desulphurization reaction, in the gas after refining, sulphur content is less than 0.5ppm.
Reaction equation is as follows:
Olefin saturated: C
2h
4+ H
2→ C
2h
6
Mercaptan: RSH+H
2→ RH+H
2s
Thioether: RSR
2+ 2H
2→ RH+R
2h+H
2s
Disulfide: RSSR
2+ 3H
2→ R1H+R
2h+2H
2s
Thiophene: C
4h
4s+4H
2→ C
4h
10+ H
2s
Carbon oxysulfide: COS+H
2→ CO+H
2s
Dithiocarbonic anhydride: CS
2+ 4H
2→ CH
4+ 2H
2s
Oxygen: O
2+ 2H
2→ 2H
2o
Unstripped gas after refining, before entering converter 8, mixes with 3.5MPa water vapor and carbon dioxide recycle gas, then is preheated to 500 DEG C through converter convection zone, enter converter radiation section by upper set pipe.Reformer tube is built with conversion catalyst, and under the effect of catalyzer, complicated conversion reaction occurs for unstripped gas and water vapour.Whole reaction process shows as strong endothermic reaction, and the heat needed for reaction is provided by the geseous fuel burner being located at converter top.Go out the pyrolytic conversion gas (temperature out is 840 DEG C) of converter after pressing steam during reforming gas vapour generator occurs, temperature is down to 350 DEG C, enters PSA unit.Concrete reaction is:
C
nH
m+nH
2O＝nCO+(n+m/2)H
2①
CO+3H
2＝CH
4+H
2O△Ho298＝-206kJ/mol②
CO+H
2O＝CO
2+H
2△Ho298＝-41kJ/mol③
3. reaction is reversible reaction, and the amount therefore by controlling carbonic acid gas in reaction gas controls the ratio of hydrogen and carbon monoxide in synthetic gas, makes it reach 2:1.
Synthetic gas from converter enters the tower (simultaneously having 1 all the time) being in absorption working condition in adsorption tower 9 at the bottom of tower, under the adsorption selection successively of multiple sorbent material wherein, removing synthesis carbonic acid gas wherein also it can be used as circulation gas to be transported in converter 8.Meanwhile, hydrogen and carbon monoxide ratio are that the synthetic gas of 2:1 enters F-T synthesis unit.
Hydrogen after purification, conversion, separation and carbon monoxide ratio are that the synthetic gas of 2:1 enters in Fischer-Tropsch synthesis device 10, generate the proper fuel oil containing many cuts through Fischer-Tropsch synthesis.
To those skilled in the art, obvious the utility model is not limited to the details of above-mentioned one exemplary embodiment, and when not deviating from spirit of the present utility model or essential characteristic, can realize the utility model in other specific forms.Therefore, no matter from which point, all should embodiment be regarded as exemplary, and be nonrestrictive, scope of the present utility model is limited by claims instead of above-mentioned explanation, and all changes be therefore intended in the implication of the equivalency by dropping on claim and scope are included in the utility model.Any Reference numeral in claim should be considered as the claim involved by limiting.
Claims (3)
1. a coke-oven gas direct production oil fuel device, comprise thionizer, compressor, pre-hydrogenator, hydrogenator, converter and Fischer-Tropsch synthesis device, it is characterized in that, described thionizer is connected in the one stage of compression import of compressor, the one stage of compression outlet of compressor is connected with TSA pretreater and PSA pretreater in turn, the outlet of PSA pretreater is connected in the two-stage compression import of compressor, the two-stage compression outlet of compressor connects pre-hydrogenator successively, hydrogenator, desulphurization reactor, converter, adsorption tower and Fischer-Tropsch synthesis device, the air outlet on described adsorption tower top is connected on the inlet mouth on the top of converter.
2. coke-oven gas direct production oil fuel device according to claim 1, is characterized in that, the gas feed on described converter top is also connected with middle pressure steam inlet pipe.
3. coke-oven gas direct production oil fuel device according to claim 1, it is characterized in that, described TSA pretreater and PSA pretreater are equipped with two.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520709433.4U CN205061981U (en) | 2015-09-14 | 2015-09-14 | Coke oven gas directly produces fuel oil device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520709433.4U CN205061981U (en) | 2015-09-14 | 2015-09-14 | Coke oven gas directly produces fuel oil device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205061981U true CN205061981U (en) | 2016-03-02 |
Family
ID=55388561
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520709433.4U Active CN205061981U (en) | 2015-09-14 | 2015-09-14 | Coke oven gas directly produces fuel oil device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205061981U (en) |
-
2015
- 2015-09-14 CN CN201520709433.4U patent/CN205061981U/en active Active
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20180511 Address after: 230000 room 1601, block C, blue ocean International Building, Shushan District, Hefei, Anhui. Patentee after: Anhui East China Chemical and Medical Engineering Co., Ltd. Address before: No. 555, No. 555, Ring Bridge Road, Shanghai, Shanghai Patentee before: Shanghai Huaxi Chemical Science & Technology Co., Ltd. |