CN202876773U - Hydrogenation reactor - Google Patents
Hydrogenation reactor Download PDFInfo
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- CN202876773U CN202876773U CN 201220592154 CN201220592154U CN202876773U CN 202876773 U CN202876773 U CN 202876773U CN 201220592154 CN201220592154 CN 201220592154 CN 201220592154 U CN201220592154 U CN 201220592154U CN 202876773 U CN202876773 U CN 202876773U
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Abstract
The utility model discloses a hydrogenation reactor. The hydrogenation reactor comprises a reactor cylinder body, a circulating oil pipe, a reactor inlet, an exhaust pipe, a mixer, a catalyst bed layer and a reactor outlet, wherein the circulating oil pipe, the mixer and the catalyst bed layer are arranged in the reactor cylinder body. The hydrogenation reactor disclosed by the utility model overcomes the defects of high investment and maintenance cost in the prior art.
Description
Technical field
The utility model relates to a kind of hydrocarbon oil hydrogenation reactor, particularly a kind of liquid phase circulation liquid phase hydrogenation reactor.
Background technology
The Powelery Solids Emission that sulfur content in the reduction diesel oil and arene content can reduce exhaust gas from diesel vehicle reduces atmosphere pollution.China's light diesel fuel specification standards are namely carried out with reference to EUROIII Emission Standard and are namely required sulphur namely to require sulphur less than 50 μ g/g less than 350 μ g/g and the execution of Europe IV standard.Be the production of reply New emission standard diesel oil, need on the one hand to solve a key technology difficult problem, newly-built hydrogenation plant carries out deep hydrodesulfurizationof of diesel oil, improves Cetane number, improves oil quality; Need to carry out comprehensive conceptual design for the enterprise practical situation on the one hand in addition, implement risk and overlapping investment and obtain preferably economic benefit to reduce.At present Petrochemical Enterprises diesel quality upgrading mostly faces diesel oil hydrogenation scarce capacity, hydrogen resource not and the problems such as the hydrogenation degree of depth is unreasonable, in the situation that the ultra-low-sulphur diesel production technology is updated, enterprise more and more tends to adopt modification scheme.Modification scheme is normally considered from following several respects: increase reactor volume (raising loaded catalyst); Select active better catalyst; Improve petroleum distribution and hydrogen cleaning in the reactor; Develop new technology etc.
In the fixed bed hydrogenation technical process of routine, in order to remove sulphur, nitrogen, oxygen, the metal impurities in the raw material or to reduce the size of feedstock, need to carry out catalytic hydrogenation reaction.For the reaction temperature of controlling beds with avoid the catalyst carbon deposit inactivation, usually adopt larger hydrogen to oil volume ratio, after finishing, hydrogenation reaction must have a large amount of hydrogen more than needed.These hydrogen more than needed mix the hydrogen feed that continues as reaction with new hydrogen usually after the circulating hydrogen compressor supercharging.This technical process also can be defined as gas phase circulation hydrogenation technique.The ratio that the investment of this process cycles hydrogen compressor accounts for whole hydrogenation plant cost is higher, hydrogen heat-exchange system energy consumption is larger, if the hydrogen flowing quantity in the hydrotreatment process can be reduced and saves hydrogen gas circulating system and circulating hydrogen compressor, can reduce investment outlay and reduce operating cost for enterprise, be that Clean Fuel Production reduces cost.Be the gas, liquid, solid three-phase in traditional fixed bed hydrogenation reactor and deposit, gas phase is the steam of hydrogen and hydrocarbon raw material, and liquid phase is the hydrocarbon raw material of vaporization not, and solid phase is catalyst.The gas-liquid liquid phase is to pass through beds with the form of drip, therefore also claims trickle bed reactor.
In trickle bed reactor, in order to strengthen the mass transfer dynamics, the volume ratio of hydrogen and feedstock oil is generally 50～2000: 1, therefore the hydrogenation reactor design is larger, and the actual feedstock oil that reacts of participating in is relevant with liquid hourly space velocity (LHSV), air speed has reflected the disposal ability of device, and larger air speed operation is adopted in industrial hope, but air speed is subject to the restriction of reaction speed.Air speed is unusual at 0.5～10h according to catalyst activity, feedstock property, reaction depth
-1Between the fluctuation.The unifining process of commercial Application can improve olefin saturated rate, hydrodesulfurization rate and hydrodenitrogeneration rate at certain reaction temperature condition decline low-speed at present.Under hydrocracking condition, improve air speed little on total conversion ratio impact, but the light component content decrease in the product is more.
The purpose that adopts the exess of H2 gas is to strengthen mass transfer and take away the amount of heat that produces because of hydrogenation reaction, and circulating hydrogen compressor is as the heart of hydrogenation process, and investment and operating cost are all higher, in order to cancel circulating hydrogen compressor
US6213835, US6428686 etc. disclose and a kind of hydrogen have been dissolved in liquid-solid two-phase hydrogenation reaction process in the liquid phase stream, feedstock oil and solvent or mixing diluents, the hydrogen that then will react required is dissolved in the mixture of feedstock oil and solvent or diluent, exists without gas phase hydrogen in the reactor.But it does not solve the H that will produce fully in the hydrofining reaction process
2S, NH
3Deng the problem that objectionable impurities removes, cause it constantly in reactor, to accumulate, greatly reduce reaction efficiency, also can't effectively process sulphur, raw material that nitrogen content is higher.In addition, the reaction system of liquid phase circulation hydrogenation technique and control method are significant to the stable operation of liquid phase circulation hydrogenation.In the disclosed liquid-phase hydrogenatin reaction system of CN200680018017.3, further control pressure and liquid level in the reactor by the amount of mixing hydrogen in the control liquid phase feeding, its weak point is in control procedure, supplemental hydrogen tolerance constantly changes with the variation of liquid level or pressure, the amounts of hydrogen that may occur replenishing is less than the situation of reacting required amounts of hydrogen, when more such as the small molecule hydrocarbon that produces under the abnormal condition, liquid level descends in the reactor, this moment, the regulative mode of control system was the mixed hydrogen amount that reduces in the liquid phase feed, if reduce too much, then amounts of hydrogen may be not enough to keep normal hydrogenation reaction, to the stable adverse effect of bringing of reaction.But above technique all is recycled to reactor inlet with the effluent part of reactor as recycle oil, if a plurality of reactor series connection, it also is the entrance that the effluent of each reactor is recycled to this reactor, another part and hydrogen mixed-shaped resulting mixture flow to into next reactor, this circulation is partial circulating, be characterized in, the reaction effluent of each reactor, a part enters into this reactor inlet as the recycle oil of this reaction, another part enters into next reactor inlet, such result is that each reactor must be equipped with an oil circulating pump, the logistics of this reactor is recycled to reactor inlet, this reactor effluent is recycled to this reactor inlet, responseless part can further be carried out the reaction second time in this recycle oil in being recycled to reactor, for fresh feed, just formed like this competitive reaction, the chain carrier of competition catalyst, thus reduce reaction efficiency.
In order to overcome the defective of this technology, Chinese patent zl20081041352.3 discloses a kind of liquid-solid two-phase hydrogenation method, a plurality of tandem reactors are placed into a catalyst in reactor divide the bed filling, hydrogen is flowed with fresh feed oil and recycle oil mixed-shaped resulting mixture in the presence of solvent or diluent, mixture flows to into reactor, another part or whole recycle oil mix with hydrogen, one the tunnel or along separate routes enter reactor between the beds, reaction effluent carries out gas-liquid separation, Partial Liquid Phase is as recycle oil, another part is isolated solvent or diluent, product liquid is as product, contain 0.1～15 volume % gas in the reactor long-pending in overall reactor, hydrogen in solvent or diluent solubility greater than the solubility of hydrogen in fresh feed oil and solvent or diluent mixture.
The circulation pipe of ZL20081041352.3 is arranged on outside the reactor, and is so just higher to the pipeline requirement, requires pipeline can bear the pressure of high pressure, has good decay resistance, and such pipeline needs larger investment and maintenance cost.
The utility model content
The present invention proposes a kind of hydrogenation reactor and has overcome prior art investment and the high defective of maintenance cost, have invest and maintenance cost little, flexible operation is easy.
A kind of hydrogenation reactor is comprised of reactor shell, circulating pipe, reactor inlet, blast pipe, blender, beds, reactor outlet, is characterised in that: circulating pipe, blender and beds arrange in the reactor shell.
Described circulating pipe one end is communicated with the reaction effluent pipe, and the other end is communicated with the reactor inlet pipe.
Described circulating pipe, blender and beds arrange in the reactor shell.
Described blender is provided with mixer outlet, mixer entrance and blast pipe.
Described mixer outlet is communicated with beds.
Described reactor outlet is communicated with the reactor outlet pipe, and the reactor outlet pipe is communicated with control valve one end, and the control valve other end is communicated with the reaction effluent pipe.
Compared with prior art, a kind of hydrogenation reactor of the utility model has compact conformation, investment and operating cost few, characteristics easy and simple to handle.
Description of drawings
Fig. 1 is a kind of hydrogenation reactor structure chart of the utility model
Fig. 2 is the another kind of hydrogenation reactor structure chart of the utility model
Wherein:
1. reactor shell, 2. circulating pipe, 3. mixer entrance, 4. reactor inlet, 5. reactor inlet pipe, 6. hydrocarbon ils, 7. hydrogen, 8. blast pipe, 9. gas, 10. blender, 11. mixer outlet, 12. mixer outlet pipes, 13. mixtures, 14. beds, 15. reactor outlets, 16. reactor outlet pipes, 17. the reaction effluent pipe, 18. product pipes, 19. control valves.
The specific embodiment
As shown in Figure 1, a kind of single beds hydrogenation reactor, by reactor shell, circulating pipe, reactor inlet, blast pipe, blender, beds, reactor outlet forms, be characterised in that: circulating pipe, blender and beds arrange in the reactor shell, circulating pipe one end is communicated with the reaction effluent pipe, the other end is communicated with the reactor inlet pipe, circulating pipe, blender and beds arrange in the reactor shell, blender is provided with mixer outlet, mixer entrance and blast pipe, described mixer outlet is communicated with beds, reactor outlet is communicated with the reactor outlet pipe, the reactor outlet pipe is communicated with control valve one end, and the control valve other end is communicated with the reaction effluent pipe.
The reaction feed of hydrogen, feedstock oil and recycle oil enters and forms mixture in the blender in the reactor and flow to into beds and contact with catalyst, beds is immersed in the liquid phase, mix amounts of hydrogen in the logistics and be under the reaction condition saturated molten hydrogen amount of mixing logistics 1～30 times.Reaction feed enters and forms mixture in the blender in the reactor and flow to into beds and catalyst haptoreaction, removes impurity wherein, and reaction effluent as recycle oil, is product through the gas-liquid separation rear section partly.
Be illustrated in figure 2 as a kind of multi-catalyst bed hydrogenation reactor, by reactor shell, circulating pipe, reactor inlet, blast pipe, blender, at least 2 beds, reactor outlet forms, circulating pipe, blender and beds arrange in the reactor shell, circulating pipe one end is communicated with the reaction effluent pipe, the other end is communicated with the reactor inlet pipe, circulating pipe, blender and beds arrange in the reactor shell, blender is provided with mixer outlet, mixer entrance and blast pipe, described mixer outlet is communicated with beds, reactor outlet is communicated with the reactor outlet pipe, the reactor outlet pipe is communicated with control valve one end, and the control valve other end is communicated with the reaction effluent pipe.
The reaction feed of hydrogen, feedstock oil and recycle oil enters and forms mixture in the blender in the reactor and flow to into beds and contact with catalyst, another part or whole recycle oil mix the molten hydrogen mixture of formation and enter reactor between the beds with hydrogen, reaction effluent through the gas-liquid separation rear section as recycle oil, part is product, beds is immersed in the liquid phase, mix amounts of hydrogen in the logistics and be under the reaction condition saturated molten hydrogen amount of mixing logistics 1～30 times.
Claims (6)
1. a hydrogenation reactor is comprised of reactor shell, circulating pipe, reactor inlet, blast pipe, blender, beds, reactor outlet, is characterised in that: circulating pipe, blender and beds arrange in the reactor shell.
2. according to a kind of hydrogenation reactor claimed in claim 1, it is characterized in that: described circulating pipe one end is communicated with the reaction effluent pipe, and the other end is communicated with the reactor inlet pipe.
3. according to a kind of hydrogenation reactor claimed in claim 1, it is characterized in that: described circulating pipe, blender and beds arrange in the reactor shell.
4. according to a kind of hydrogenation reactor claimed in claim 1, it is characterized in that: described blender is provided with mixer outlet, mixer entrance and blast pipe.
5. according to a kind of hydrogenation reactor claimed in claim 1, it is characterized in that: described mixer outlet is communicated with beds.
6. according to a kind of hydrogenation reactor claimed in claim 1, it is characterized in that: described reactor outlet is communicated with the reactor outlet pipe, and the reactor outlet pipe is communicated with control valve one end, and the control valve other end is communicated with the reaction effluent pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220592154 CN202876773U (en) | 2012-11-02 | 2012-11-02 | Hydrogenation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220592154 CN202876773U (en) | 2012-11-02 | 2012-11-02 | Hydrogenation reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202876773U true CN202876773U (en) | 2013-04-17 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220592154 Expired - Lifetime CN202876773U (en) | 2012-11-02 | 2012-11-02 | Hydrogenation reactor |
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| Country | Link |
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| CN (1) | CN202876773U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105503521A (en) * | 2016-02-23 | 2016-04-20 | 上海华谊（集团）公司 | Method for preparing ethyl alcohol by acetic acid hydrogenation |
-
2012
- 2012-11-02 CN CN 201220592154 patent/CN202876773U/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105503521A (en) * | 2016-02-23 | 2016-04-20 | 上海华谊（集团）公司 | Method for preparing ethyl alcohol by acetic acid hydrogenation |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20130417 |
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| CX01 | Expiry of patent term |