CN202530049U - Liquid phase hydrogenation reaction system device - Google Patents
Liquid phase hydrogenation reaction system device Download PDFInfo
- Publication number
- CN202530049U CN202530049U CN2012200743104U CN201220074310U CN202530049U CN 202530049 U CN202530049 U CN 202530049U CN 2012200743104 U CN2012200743104 U CN 2012200743104U CN 201220074310 U CN201220074310 U CN 201220074310U CN 202530049 U CN202530049 U CN 202530049U
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- liquid
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- reaction product
- reaction
- liquid phase
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- 239000007791 liquid phase Substances 0.000 title claims abstract description 47
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 39
- 239000001257 hydrogen Substances 0.000 claims abstract description 32
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 32
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 31
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 27
- 238000006243 chemical reaction Methods 0.000 claims abstract description 18
- 238000000034 method Methods 0.000 claims abstract description 16
- 239000007789 gas Substances 0.000 claims description 17
- 239000007788 liquid Substances 0.000 claims description 15
- 239000000463 material Substances 0.000 claims description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 9
- 229910052717 sulfur Inorganic materials 0.000 abstract description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 6
- 239000012071 phase Substances 0.000 abstract description 5
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 abstract description 4
- 229910021529 ammonia Inorganic materials 0.000 abstract description 4
- 229910000037 hydrogen sulfide Inorganic materials 0.000 abstract description 4
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 2
- 239000000446 fuel Substances 0.000 abstract description 2
- 239000011593 sulfur Substances 0.000 abstract description 2
- 229910000069 nitrogen hydride Inorganic materials 0.000 abstract 3
- 230000001105 regulatory effect Effects 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model discloses a liquid phase hydrogenation reaction system device, which is used for solving the problem of H in the inlet of a reactor2S and NH3The method is designed for continuously accumulating to inhibit the depth of hydrogenation reaction, namely, a reaction product stripping tower is added on the basis of the existing liquid phase hydrogenation process, the circulating reaction product at the outlet of the liquid phase hydrogenation reactor enters the reaction product stripping tower after being reduced in pressure through a regulating valve, hydrogen is introduced into the stripping tower through a hydrogen inlet pipeline at the bottom of the tower, and the reaction product is treated by the stripping towerH in (1)2S and NH3The oil phase at the bottom of the tower is stripped out and returns to the inlet of the liquid phase hydrogenation reactor after the pressure of the reaction product circulating pump is increased, thus effectively eliminating the hydrogen sulfide and ammonia brought in by the circulating liquid phase2S and NH3) The influence on a reaction system improves the reaction efficiency and obtains the clean fuel with low sulfur and nitrogen.
Description
Technical field
The utility model relates to a kind of liquid-phase hydrogenatin reactive system device, belongs to the hydrogen addition technology field.
Background technology
The liquid-phase hydrogenatin Technology is a novel hydrogen addition technology.Reactions such as the desulfurization of conventional trickle bed hydrogenator, denitrogenation are mainly with the hydrogen mass transfer, and promptly hydrogen is the controlled step of whole hydrogenation reaction from gas phase diffusion and the speed that is dissolved into the oil.The characteristics of liquid-phase hydrogenatin technology then are to eliminate the influence of hydrogen mass transfer; Hydrogenation reaction is carried out in the kinetic control district, and soon hydrogen is dissolved in and satisfies the required hydrogen of hydrogenation reaction in the raw oil, is pure liquid phase reaction in reactor drum; Can eliminate the mass transport affects of hydrogen from the gas phase to the liquid phase; Through the hydrogen of liquid circulation dissolving capacity, satisfy the needs of hydrogenation reaction, save investment of devices such as circulating hydrogen compressor and HP separator.Compare with traditional trickle bed technology; Hydrogen gas circulating system and Separate System of Water-jet are not set in the liquid-phase hydrogenatin technical process; And increased the static mixer of the liquid phase recycle system and hydrogen and oil; Be dissolved in the charging fully with assurance hydrogen, and the material in reactor drum exists with pure liquid phase state.
But in present liquid-phase hydrogenatin technical process; Because hydrogenation reaction needs a large amount of hydrogen; Institute's dissolved hydrogen still can't satisfy the demands in the fresh feed oil and only depend on; Therefore in technical process, be provided with the reaction product recycle pump, a large amount of reaction product is circulated to reactor inlet by reactor outlet, provide hydrogenation reaction needed hydrogen.Yet, because through containing the H that hydrogenation reaction generates in the hydrogenation reaction afterreaction product
2S and NH
3, after it is circulated to reactor inlet and fresh feed oil mixes, will cause containing in the reactor inlet logistics a large amount of H
2S and NH
3In view of the principle of chemical reaction equilibrium, H
2S and NH
3Existence will suppress the carrying out of hydrodesulfurization reaction and denitrification reaction, the production difficulty of the product that sulphur content that causes stipulating in the V standard of Europe and nitrogen content are 10 μ g/g.
CN200910204293.4 discloses a kind of reactor drum and liquid-phase hydrogenatin process method; This reactor drum comprises at least two beds; For removing hydrogen sulfide and the ammonia that reaction generates; Between at least one adjacent catalyst bed layer, be provided with the inner member of complicated gas make-up and the impure excess air of discharging, Equipment Design and processing are brought difficulty.
CN201010001103.1 discloses a kind of circulation fluid phase method of hydrotreating, and this method is through being provided with the liquid phase of thermal high separating tank and thermal low separating tank partitioning cycle, though can partly isolate hydrogen sulfide and ammonia, separating effect is undesirable.
Summary of the invention
The purpose of the utility model is to provide a kind of liquid-phase hydrogenatin reactive system device, and it can effectively solve H in the reactor inlet
2S and NH
3Constantly accumulate and the problem of the inhibition hydrogenation reaction degree of depth.
The concrete technical scheme of the utility model is following:
Reaction feed furnace outlet pipeline is communicated with the gas liquid mixer inlet; The gas liquid mixer outlet line is communicated with the liquid phase hydrogenation reactor inlet; The liquid phase hydrogenation reactor outlet line is communicated with reaction product stripping tower inlet, and the stripping tower source line is provided with pressure regulator valve, and the stripping tower outlet line is communicated with gas liquid mixer through the reaction product recycle pump, and the stripping tower bottom is communicated with into the hydrogen pipeline;
The benefit hydrogen pipeline that make-up hydrogen compressor is set can be communicated with gas liquid mixer and liquid phase hydrogenation reactor;
Raw oil surge tank and hydrogenation fresh feed pump can be communicated with liquid-phase hydrogenatin reactive system device, and are communicated with benefit hydrogen pipeline simultaneously;
Raw oil/reaction product interchanger can be connected between hydrogenation fresh feed pump and the reaction feed process furnace, and the liquid phase hydrogenation reactor outlet line can be communicated with the thermal material pipeline of raw oil/reaction product interchanger.
The utility model device liquid-phase hydrogenatin reactive system device has increased a reaction product stripping tower on the basis of existing liquid-phase hydrogenatin flow process, the circulating reaction product of liquid phase hydrogenation reactor outlet is through getting into the reaction product stripping tower after the variable valve step-down.The go into hydrogen pipeline of stripping tower at the bottom of through tower feeds hydrogen, with the H in the reaction product
2S and NH
3Stripping comes out, and returns the liquid phase hydrogenation reactor inlet after the oil phase at the bottom of the tower then boosts through the reaction product recycle pump, has so just effectively eliminated hydrogen sulfide and the ammonia (H that brings in the circulation liquid phase
2S and NH
3) to the influence of reactive system, improve reaction efficiency, obtain the clean fuel of low-sulfur and low nitrogen.
Description of drawings
Fig. 1 is a liquid-phase hydrogenatin reactive system device syndeton synoptic diagram.
Fig. 2 is existing liquid-phase hydrogenatin reaction unit syndeton synoptic diagram.
Embodiment
Embodiment:
With reference to Fig. 1 and 2 the embodiment of the utility model is further specified:
Reaction feed process furnace 4 outlet lines are communicated with gas liquid mixer 10 inlets; Gas liquid mixer 10 outlet lines are communicated with liquid phase hydrogenation reactor 5 inlets; Liquid phase hydrogenation reactor 5 outlet lines are communicated with reaction product stripping tower 8 inlets, and stripping tower 8 source lines are provided with pressure regulator valve 9, and stripping tower 8 outlet lines are communicated with gas liquid mixer 10 through reaction product recycle pump 6, and stripping tower 8 bottoms are communicated with into the hydrogen pipeline; According to actual needs, reaction product recycle pump 6 outlet lines also can be communicated with gas liquid mixer 10 again after reaction feed process furnace 4 outlet lines merge.
When the hydrogen make-up insufficient pressure, can the benefit hydrogen pipeline that make-up hydrogen compressor 7 is set be communicated with gas liquid mixer 10 and liquid phase hydrogenation reactor 5;
When the hydrogenation feed pressure is not enough, can the hydrogenation feeding line be communicated with liquid-phase hydrogenatin reactive system device through raw oil surge tank 1 and hydrogenation fresh feed pump 2, and be communicated with benefit hydrogen pipeline simultaneously.
Raw oil/reaction product interchanger 3 can be connected between hydrogenation fresh feed pump 2 and the reaction feed process furnace 4; Liquid phase hydrogenation reactor 5 outlet lines can be communicated with the thermal material pipeline of raw oil/reaction product interchanger 3; Can pass through raw oil/reaction product interchanger 3 and reclaim the heat of liquid phase hydrogenation reactor 5 outlet logistics, with the raw oil of heating hydrogenation fresh feed pump 2 outlets.
Claims (5)
1. liquid-phase hydrogenatin reactive system device is characterized in that:
Reaction feed process furnace (4) outlet line is communicated with gas liquid mixer (10) inlet; Gas liquid mixer (10) outlet line is communicated with liquid phase hydrogenation reactor (5) inlet; Liquid phase hydrogenation reactor (5) outlet line is communicated with reaction product stripping tower (8) inlet; Stripping tower (8) source line is provided with pressure regulator valve (9); Stripping tower (8) outlet line is communicated with gas liquid mixer (10) through reaction product recycle pump (6), and stripping tower (8) bottom is communicated with into the hydrogen pipeline.
2. liquid-phase hydrogenatin reactive system device as claimed in claim 1, it is characterized in that reaction product recycle pump (6) outlet line can be communicated with gas liquid mixer (10) again after reaction feed process furnace (4) outlet line merges.
3. liquid-phase hydrogenatin reactive system device as claimed in claim 1 is characterized in that the benefit hydrogen pipeline that make-up hydrogen compressor (7) is set can be communicated with gas liquid mixer (10) and liquid phase hydrogenation reactor (5).
4. liquid-phase hydrogenatin reactive system device as claimed in claim 1 is characterized in that raw oil surge tank (1) and hydrogenation fresh feed pump (2) can be communicated with liquid-phase hydrogenatin reactive system device, and is communicated with benefit hydrogen pipeline simultaneously.
5. liquid-phase hydrogenatin reactive system device as claimed in claim 1; It is characterized in that raw oil/reaction product interchanger (3) can be connected between hydrogenation fresh feed pump (2) and the reaction feed process furnace (4), liquid phase hydrogenation reactor (5) outlet line can be communicated with the thermal material pipeline of raw oil/reaction product interchanger (3).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012200743104U CN202530049U (en) | 2012-03-01 | 2012-03-01 | Liquid phase hydrogenation reaction system device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012200743104U CN202530049U (en) | 2012-03-01 | 2012-03-01 | Liquid phase hydrogenation reaction system device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202530049U true CN202530049U (en) | 2012-11-14 |
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ID=47131245
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012200743104U Expired - Lifetime CN202530049U (en) | 2012-03-01 | 2012-03-01 | Liquid phase hydrogenation reaction system device |
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|---|---|
| CN (1) | CN202530049U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014117309A1 (en) * | 2013-01-30 | 2014-08-07 | 中国石油天然气股份有限公司 | Liquid-phase hydrogenation reaction method for multi-stage hydrogen dissolution |
| CN105524657A (en) * | 2014-09-29 | 2016-04-27 | 中国石油化工股份有限公司 | Method for hydrogenation of distillate oil via fluidized bed |
| CN111019696A (en) * | 2018-10-09 | 2020-04-17 | 中石化广州工程有限公司 | Hydrotreater |
| CN114437809A (en) * | 2020-11-05 | 2022-05-06 | 中国石油天然气集团有限公司 | Liquid-phase hydrogenation device and liquid-phase hydrogenation method |
-
2012
- 2012-03-01 CN CN2012200743104U patent/CN202530049U/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014117309A1 (en) * | 2013-01-30 | 2014-08-07 | 中国石油天然气股份有限公司 | Liquid-phase hydrogenation reaction method for multi-stage hydrogen dissolution |
| CN105524657A (en) * | 2014-09-29 | 2016-04-27 | 中国石油化工股份有限公司 | Method for hydrogenation of distillate oil via fluidized bed |
| CN105524657B (en) * | 2014-09-29 | 2017-03-29 | 中国石油化工股份有限公司 | A kind of fraction oil boiling bed hydrogenation method |
| CN111019696A (en) * | 2018-10-09 | 2020-04-17 | 中石化广州工程有限公司 | Hydrotreater |
| CN114437809A (en) * | 2020-11-05 | 2022-05-06 | 中国石油天然气集团有限公司 | Liquid-phase hydrogenation device and liquid-phase hydrogenation method |
| CN114437809B (en) * | 2020-11-05 | 2023-12-22 | 中国石油天然气集团有限公司 | Liquid phase hydrogenation device and liquid phase hydrogenation method |
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|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20121114 |
|
| CX01 | Expiry of patent term |