CN204643834U - A kind of for petroleum products hydrorefined hydrogen raw material production equipment - Google Patents
A kind of for petroleum products hydrorefined hydrogen raw material production equipment Download PDFInfo
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- CN204643834U CN204643834U CN201520229923.4U CN201520229923U CN204643834U CN 204643834 U CN204643834 U CN 204643834U CN 201520229923 U CN201520229923 U CN 201520229923U CN 204643834 U CN204643834 U CN 204643834U
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- 239000001257 hydrogen Substances 0.000 title claims abstract description 225
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 225
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 214
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 127
- 239000002994 raw material Substances 0.000 title claims abstract description 101
- 239000003209 petroleum derivative Substances 0.000 title claims abstract description 60
- GBMDVOWEEQVZKZ-UHFFFAOYSA-N methanol;hydrate Chemical compound O.OC GBMDVOWEEQVZKZ-UHFFFAOYSA-N 0.000 claims abstract description 127
- 239000007789 gas Substances 0.000 claims abstract description 24
- 238000003860 storage Methods 0.000 claims abstract description 22
- 238000000926 separation method Methods 0.000 claims abstract description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 70
- 229910001868 water Inorganic materials 0.000 claims description 67
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 65
- 238000010438 heat treatment Methods 0.000 claims description 47
- 238000000746 purification Methods 0.000 claims description 30
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 24
- 239000007788 liquid Substances 0.000 claims description 19
- 230000008016 vaporization Effects 0.000 claims description 18
- 238000000034 method Methods 0.000 claims description 14
- 239000012528 membrane Substances 0.000 claims description 12
- 239000007858 starting material Substances 0.000 claims description 12
- 238000009834 vaporization Methods 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 230000009183 running Effects 0.000 claims description 10
- 238000001514 detection method Methods 0.000 claims description 9
- 238000009434 installation Methods 0.000 claims description 9
- 239000000463 material Substances 0.000 claims description 9
- 229910001316 Ag alloy Inorganic materials 0.000 claims description 7
- SWELZOZIOHGSPA-UHFFFAOYSA-N palladium silver Chemical compound [Pd].[Ag] SWELZOZIOHGSPA-UHFFFAOYSA-N 0.000 claims description 7
- 238000002485 combustion reaction Methods 0.000 claims description 6
- 238000002309 gasification Methods 0.000 claims description 5
- 230000003139 buffering effect Effects 0.000 claims description 3
- 239000000919 ceramic Substances 0.000 claims description 3
- 238000000576 coating method Methods 0.000 claims description 3
- 230000007423 decrease Effects 0.000 claims description 3
- 238000012423 maintenance Methods 0.000 claims description 3
- 238000001771 vacuum deposition Methods 0.000 claims description 3
- 150000002431 hydrogen Chemical class 0.000 abstract description 10
- 238000010586 diagram Methods 0.000 description 8
- 239000003921 oil Substances 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 7
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 4
- 238000007670 refining Methods 0.000 description 4
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000010276 construction Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000003208 petroleum Substances 0.000 description 3
- 238000006057 reforming reaction Methods 0.000 description 3
- 239000003381 stabilizer Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 230000002159 abnormal effect Effects 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 235000011089 carbon dioxide Nutrition 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000023556 desulfurization Effects 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 229910052763 palladium Inorganic materials 0.000 description 2
- 238000002407 reforming Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 239000005662 Paraffin oil Substances 0.000 description 1
- 206010033799 Paralysis Diseases 0.000 description 1
- BQCADISMDOOEFD-UHFFFAOYSA-N Silver Chemical compound [Ag] BQCADISMDOOEFD-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000002199 base oil Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 125000005842 heteroatom Chemical group 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 229910052709 silver Inorganic materials 0.000 description 1
- 239000004332 silver Substances 0.000 description 1
- 238000002207 thermal evaporation Methods 0.000 description 1
Landscapes
- Hydrogen, Water And Hydrids (AREA)
Abstract
The utility model discloses a kind of for petroleum products hydrorefined hydrogen raw material production equipment, comprise control device, methanol-water Storing and conveying device and at least three group methanol-water reformation hydrogen production modules, control device and methanol-water Storing and conveying device and each organize methanol-water reformation hydrogen production module and be all electrically connected, to control the working order of methanol-water Storing and conveying device and each group methanol-water reformation hydrogen production module; The obtained hydrogen of each group of methanol-water reformation hydrogen production module directly sends petroleum products hydrofining system to by transport pipe, and control device operates according to the methanol-water reformation hydrogen production module of the hydrogen raw materials requirement amount information Control proper amt of petroleum products hydrofining system.The utility model modularization is high, and single module volume is little, start fast, need not hydrogen-storage tank, instant hydrogen manufacturing and sharp separation can go out hydrogen, good stability, intelligent high, the aspect state modulator such as hydrogen manufacturing temperature, gas flow and air pressure are sensitive, and security is high, reliability is strong.
Description
Technical field
The utility model relates to refining of petroleum, petrochemical complex and energy technology field, and particularly one is used for petroleum products hydrorefined hydrogen raw material production equipment.
Background technology
Petroleum products hydrofining, its objective is heteroatoms and the metallic impurity etc. such as sulphur, nitrogen, oxygen in removing oil product, and to part aromatic hydrocarbons or olefins hydrogenation, improves the use properties of oil product.Petroleum products hydrofining can be used for the refining of gasoline, kerosene, diesel oil, lubricating oil, paraffin oil, various intermediate oil, heavy oil and residual oil.In addition, it is saturated that hydrogen can also be used for the partial hydrogenation of aromatic hydrocarbons in rocket engine fuel, the hydrogenating desulfurization of oil fuel, residual oil removing heavy-metal and diasphaltene pre-treatment etc.Various oil hydrogenation process for refining flow process is substantially identical, after stock oil mixes with hydrogen, sends into heating tower and is heated to specified temperature, then enter and be equipped with in the reactor of catalyzer; After having reacted, hydrogen separates in the separator, and recycles through compressor; The gaseous hydrogen that petroleum products then separates hydrogen sulfide, ammonia, water and decomposes on a small quantity in reaction process and produce in stabilizer tower.
In the prior art, petroleum products hydrorefined hydrogen raw material sources mainly contain three kinds: one, the directly canned hydrogen of buying; Two, take petroleum products as waste hydrogen, such as Chinese invention application 02109678.3 and 02109679.1 all relates to directly use raw gasline preparing hydrogen, these class methods need to consume petroleum products natively very in short supply, and this kind of hydrogen producer volume is large, startup is slow, intellectuality is low, poor stability, energy consumption are high; Three, with the mixing dry gas of petroleum refinery for unstripped gas prepares hydrogen, with reference to Chinese invention application 200510046170.4, it is that the mixing dry gas of residual hydrogenation, hydrofining, hydrocracking and diesel hydrotreating unit being discharged sends into hydrogen making in device for producing hydrogen through compressor pressurization, these class methods can fully reclaim hydrogen in mixing dry gas, but the amounts of hydrogen reclaimed is very limited, still needs to take petroleum products as waste hydrogen.
Along with the progress of technology, adopt the technology of first alcohol and water reformation hydrogen production to be developed gradually, this hydrogen obtained by first alcohol and water reforming hydrogen producing technology is used as the unstripped gas in petroleum products hydrofining industry gradually.With reference to Chinese invention application 201310340475.0(applicant: Shanghai Hejide Dynamic Hydrogen Machine Co., Ltd.), which disclose a Methanol water hydrogen production system, the reformer chamber of methyl alcohol and steam reformer, at 350-409 DEG C of temperature 1-5M Pa pressure condition under pass through catalyzer, under the effect of catalyzer, the transformationreation of methanol decomposition reaction and carbon monoxide occurs, generates hydrogen and carbonic acid gas, this is the gas solid catalytic reaction system of component more than, many reactions.Reactional equation is as follows: (1) CH
3oH → CO+2H
2; (2) H
2o+CO → CO
2+ H
2; (3) CH
3oH+H
2o → CO
2+ 3H
2, the H that reforming reaction generates
2and CO
2, then the palladium membrane separation apparatus through separate chamber is by H
2and CO
2be separated, obtain high-purity hydrogen.But in existing petroleum products unifining process, methanol-water reforming hydrogen producing technology all adopts single reformer, intelligent poor, cannot modularization, volume large, start slowly, methanol feedstock waste is serious, security is low, whole process need hydrogen-storage tank, the hydrorefined stability of petroleum products is difficult to ensure.
Utility model content
The technical problems to be solved in the utility model is for above-mentioned deficiency of the prior art, there is provided a kind of for petroleum products hydrorefined hydrogen raw material production equipment, this hydrogen raw material production EM equipment moduleization is high, single module volume is little, startup is quick, need not hydrogen-storage tank, instant hydrogen manufacturing and sharp separation can go out hydrogen, good stability, intelligent high, the aspect state modulator such as hydrogen manufacturing temperature, gas flow and air pressure are sensitive, and security is high, reliability is strong.
For solving the problems of the technologies described above, the technical solution of the utility model is:
A kind of for petroleum products hydrorefined hydrogen raw material production equipment, comprise control device, methanol-water Storing and conveying device and at least three group methanol-water reformation hydrogen production modules, described control device and methanol-water Storing and conveying device and each organize methanol-water reformation hydrogen production module and be all electrically connected, to control the working order of methanol-water Storing and conveying device and each group methanol-water reformation hydrogen production module; The hydrogen that described each group of methanol-water reformation hydrogen production module obtains directly sends petroleum products hydrofining system to by transport pipe, this petroleum products hydrofining system is in hydrorefined process, instant hydrogen raw materials requirement amount is fed back to control device, this control device operates according to the methanol-water reformation hydrogen production module of the hydrogen raw materials requirement amount information Control proper amt of petroleum products hydrofining system, and controls the methanol-water reformation hydrogen production module conveying first alcohol and water raw material of methanol-water Storing and conveying device to running.
Described methanol-water Storing and conveying device comprises methanol-water storage vessel and transferpump, store liquid first alcohol and water raw material in described methanol-water storage vessel, described transferpump is used for the first alcohol and water feedstock transportation in methanol-water storage vessel to methanol-water reformation hydrogen production module; The quantity of described transferpump and the quantity of methanol-water reformation hydrogen production module match, and the quantity of described methanol-water storage vessel is equal to or less than the quantity of transferpump.
Described methanol-water reformation hydrogen production module comprises reformer, reformer chamber and hydrogen purification apparatus is provided with in this reformer, the temperature of reformer chamber is 300-570 DEG C of temperature, reformer chamber is provided with catalyzer, first alcohol and water is at the obtained hydrogen-containing gas of reformation hydrogen production reaction of reformer chamber generation first alcohol and water, reformer chamber is connected by connecting pipeline with hydrogen purification apparatus, and all or part of of connecting pipeline is arranged at reformer chamber, and the high temperature by reformer chamber continues the gas that heating exports from reformer chamber; Described connecting pipeline is as the buffering between reformer chamber and hydrogen purification apparatus, make the temperature of the gas exported from reformer chamber identical with the temperature of hydrogen purification apparatus or close, obtain hydrogen from the aerogenesis end of hydrogen purification apparatus, be supplied to petroleum products hydrofining system.
Described methanol-water reformation hydrogen production module comprises two kinds of preferred structure modes:
The preferred structure mode of the first methanol-water reformation hydrogen production module is: described methanol-water reformation hydrogen production module is integrated with interchanger, described interchanger is installed on the transport pipe between methanol-water Storing and conveying device and reformer, the first alcohol and water raw material of low temperature is in interchanger, the high-temperature gas exported with reformer chamber carries out heat exchange, and first alcohol and water material temperature raises, vaporization; Described reformer is provided with electric heater, and this electric heater provides 300-570 DEG C of temperature for reformer chamber; The hydrogen of the aerogenesis end output of described hydrogen purification apparatus, after interchanger, temperature reduces, then is supplied to petroleum products hydrofining system.
Further, be also provided with compensation vapourizing unit between described interchanger and reformer, this compensation vapourizing unit is provided with electric heater, and described first alcohol and water raw material can be vaporized further after compensating vapourizing unit.
The preferred structure mode of the second methanol-water reformation hydrogen production module is: described methanol-water reformation hydrogen production module is integrated with interchanger, described interchanger is installed on the transport pipe between methanol-water Storing and conveying device and reformer, the first alcohol and water raw material of low temperature is in interchanger, the high-temperature gas exported with reformer chamber carries out heat exchange, and first alcohol and water material temperature raises, vaporization; Also vaporizing chamber is not had in described reformer, described first alcohol and water raw material enters vaporizing chamber vaporization in interchanger after heat exchange, methanol steam after vaporization and water vapor enter reformer chamber, and reformer chamber bottom and middle portion temperature are 300-420 DEG C, and the temperature on reformer chamber top is 400-570 DEG C; The all or part of top being arranged at reformer chamber of the connecting pipeline between described reformer chamber and hydrogen purification apparatus; The hydrogen of the aerogenesis end output of described hydrogen purification apparatus, after interchanger, temperature reduces, then is supplied to petroleum products hydrofining system.
Further, described reformer one end is provided with starter gear, and this starter gear comprises cup, cup is provided with raw material input channel, heating and gasifying pipeline, portfire and temperature detection device; Described raw material input channel can input first alcohol and water raw material, and raw material input channel is connected with heating and gasifying pipeline, and first alcohol and water raw material enters after heating and gasifying pipeline through raw material input channel, exports from the end of heating and gasifying pipeline; The position of described portfire is corresponding with the end of heating and gasifying pipeline, for lighting a fire to the first alcohol and water raw material exported in heating and gasifying pipeline, first alcohol and water raw material is through ignition device afterfire, can heat heating and gasifying pipeline, make heating and gasifying ducted first alcohol and water material gasification and strengthen rapidly intensity of combustion, and then being reformer heating; Described temperature detection device is for detecting the other temperature of heating and gasifying pipeline; After described reformer starts hydrogen manufacturing, the hydrogen partial that reformer is obtained is or/and residual air is run by burning maintenance reformer.
Further again, described cup comprises the liquid containing portion above installation portion and installation portion, described raw material input channel, heating and gasifying pipeline, portfire and temperature detection device are all installed on the installation portion of cup, described liquid containing portion can hold the first alcohol and water raw material exported from heating and gasifying pipe end, and described liquid containing portion upper end is also provided with liquid Splashproof cover; Described heating and gasifying pipeline comprises straight-through pipeline section, pigtail and upper arch pipeline section successively, and described first alcohol and water raw material after straight-through pipeline section rises to extreme higher position, then can decline through pigtail spiral, then exports after upper arch pipeline section; The bottom side of described cup is provided with air intake cover plate, and this air intake cover plate is provided with air channel, and outside air can enter in reformer through this air channel; Described raw material input channel is provided with magnetic valve, opens or closes to control raw material input channel.
In technique scheme, described hydrogen purification apparatus is membrane separation unit, and this membrane separation unit is the membrane separation unit at porous ceramic surface Vacuum Deposition palladium-silver alloy, and coatings is palladium-silver alloy.
The beneficial effects of the utility model are:
One, the utility model adopt at least three group methanol-water reformation hydrogen production modules, and the degree of modularity is high, and single methanol-water reformation hydrogen production modular volume is little, startup is quick, and the aspect state modulator such as hydrogen manufacturing temperature, gas flow and air pressure are sensitive;
The hydrogen that two, the utility model respectively organizes methanol-water reformation hydrogen production module obtained directly sends petroleum products hydrofining system to by transport pipe, without the need to high pressure hydrogen storage containers such as hydrogen-storage tanks, the instant hydrogen manufacturing of energy and sharp separation go out hydrogen, thus eliminate hydrogen-storage tank cost, improve the degree of safety of hydrogen conveying, avoid the hydrogen leak even problem of hydrogen-storage tank blast that cause because hydrogen-storage tank is abnormal;
Three, due to the utility model, often to organize the hydrogen manufacturing amount of methanol-water reformation hydrogen production module much smaller relative to the hydrogen manufacturing amount of methanol-water reformation hydrogen production module single in prior art, such as, if the utility model arranges 100 groups of methanol-water reformation hydrogen production modules, the hydrogen manufacturing amount that so the utility model often organizes methanol-water reformation hydrogen production module only needs 1/100 of the hydrogen manufacturing amount of single methanol-water reformation hydrogen production module in prior art; When instant hydrogen raw materials requirement amount is less, control device only needs to control less methanol-water reformation hydrogen production module (such as 50 groups) running; Therefore, when the utility model adopts at least three group methanol-water reformation hydrogen production modules as hydrogen manufacturing agent set, greatly can reduce zero load, its overall power consumption is less, and first alcohol and water raw material consumption is lower, utilization ratio is high;
After four, the utility model adopts at least three group methanol-water reformation hydrogen production modules, when one group of methanol-water reformation hydrogen production module breaks down, other methanol-water reformation hydrogen production modules of hydrogen raw material production equipment can also run well, or the methanol-water reformation hydrogen production module replacement work being in holding state can be made, therefore, its stability and reliability is good, intelligent high, can prevent the great exception causing petroleum products hydrofining system because of the paralysis of part methanol-water reformation hydrogen production module;
Five, the methanol-water reformation hydrogen production module noise of less hydrogen manufacturing amount is less, is conducive to reducing sound pollution;
Six, the utility model adopts at least three group methanol-water reformation hydrogen production modules, when methanol-water reformation hydrogen production module quantity is inadequate, methanol-water reformation hydrogen production module can be increased easily, improve hydrogen manufacturing amount, make methanol-water reformation hydrogen production module quantity of the present utility model energy masterly ground resilient expansion;
After seven, the present invention arranges at least three group methanol-water reformation hydrogen production modules, the hydrogen delivery tube road that single methanol-water reformation hydrogen production module is sent to petroleum products hydrofining system can be accomplished very little, the hydrogen delivery tube road of this very minor diameter significantly can improve its ability of bearing pressure, and (pipeline is less, bearing capacity is larger), thus significantly improve the safety performance of petroleum products hydrofining system.
Accompanying drawing explanation
Fig. 1 is one-piece construction block diagram of the present utility model.
Fig. 2 is the methanol-water Storing and conveying apparatus structure block diagram of the utility model one preferred embodiment.
Fig. 3 is the methanol-water Storing and conveying apparatus structure block diagram of another preferred embodiment of the utility model.
Fig. 4 is the methanol-water reformation hydrogen production modular structure block diagram of the utility model one preferred embodiment.
Fig. 5 is the methanol-water reformation hydrogen production modular structure block diagram of another preferred embodiment of the utility model.
Fig. 6 is the dispersed texture schematic diagram of reformer in Fig. 5.
Fig. 7 is the structural representation of reformer starter gear in Fig. 5.
Fig. 8 is the cup holder portion structural representation of reformer starter gear in Fig. 5.
Fig. 9 is the one-piece construction block diagram of petroleum products hydrofining system.
Embodiment
Below in conjunction with accompanying drawing, structural principle of the present utility model and principle of work are described in further detail.
As shown in Figure 9, for the one-piece construction skeleton diagram of petroleum products hydrofining system, hydrogen and petroleum products enter reactor 7 after entering process furnace 6 Hybrid Heating, in reactor 7 catalyzer effect under, carry out petroleum products hydrofining reaction, comprise the reaction such as hydrotreated lube base oil, demetalization of desulfurization, denitrogenation, deoxidation, alkene and aromatic hydrocarbons; Then, the mixture after reaction is separated through separator 8, and unreacted hydrogen is back to the input of process furnace 6 after compressor 9 compresses, and restarts hydrofining reaction next time, and petroleum products, waste gas and low boiling hydrocarbon after refining then enter stabilizer tower 10; After stabilizer tower is stable, exports petroleum refinement product, and drain waste gas and low boiling hydrocarbon.
As shown in Figure 1, a kind of for petroleum products hydrorefined hydrogen raw material production equipment, comprise control device 1, methanol-water Storing and conveying device 2 and at least three group methanol-water reformation hydrogen production modules 3, described control device 1 is organized methanol-water reformation hydrogen production module 3 with methanol-water Storing and conveying device 2 and each and is all electrically connected, to control the working order of methanol-water Storing and conveying device 2 and each group methanol-water reformation hydrogen production module 3; The hydrogen that described each group of methanol-water reformation hydrogen production module 3 obtains directly sends petroleum products hydrofining system 4 to by transport pipe, this petroleum products hydrofining system 4 is in hydrorefined process, instant hydrogen raw materials requirement amount is fed back to control device 1, this control device 1 operates according to the methanol-water reformation hydrogen production module 3 of the hydrogen raw materials requirement amount information Control proper amt of petroleum products hydrofining system 4, and control methanol-water Storing and conveying device 2 to running methanol-water reformation hydrogen production module 3 carry first alcohol and water raw material.In addition, the quantity of the utility model methanol-water reformation hydrogen production module 3 is preferably 20 groups ~ 200 groups, more preferably 60 groups ~ 120 groups, can better ensure the hydrogen demand amount of petroleum products hydrofining system like this.
After the utility model arranges at least three group methanol-water reformation hydrogen production modules 3, the hydrogen delivery tube road that single methanol-water reformation hydrogen production module 3 is sent to petroleum products hydrofining system can be accomplished very little, hydrogen delivery tube road of the present invention adopts diameter to be the stainless steel tube of 2 ~ 8mm, the hydrogen delivery tube road of this diameter significantly can improve its ability of bearing pressure, and (pipeline is less, bearing capacity is larger), thus significantly improve the safety performance of petroleum products hydrofining system.Further, hydrogen delivery tube road is preferably and adopts diameter to be the stainless steel tube of 3 ~ 6mm.
As shown in Figures 2 and 3, described methanol-water Storing and conveying device 2 comprises methanol-water storage vessel 21 and transferpump 22, store liquid first alcohol and water raw material in described methanol-water storage vessel 21, described transferpump 22 for by the first alcohol and water feedstock transportation in methanol-water storage vessel 21 to methanol-water reformation hydrogen production module 3; The quantity of described transferpump 22 and the quantity of methanol-water reformation hydrogen production module 3 match, and the quantity of described methanol-water storage vessel 21 is equal to or less than the quantity of transferpump 22.In fig. 2, the quantity of methanol-water storage vessel 21 is independent 1, and the quantity of methanol-water storage vessel 21 and the quantity of transferpump 22 match in figure 3.
As shown in Figure 4 and Figure 5, described methanol-water reformation hydrogen production module 3 comprises reformer 31 or 32, reformer chamber 311 or 321 and hydrogen purification apparatus 312 or 322 is provided with in this reformer 31 or 32, the temperature of reformer chamber is 300-570 DEG C of temperature, reformer chamber is provided with catalyzer, in reformer chamber, methyl alcohol and water vapour pass through catalyzer under the pressure condition of 1-5M Pa, under the effect of catalyzer, there is the transformationreation of methanol decomposition reaction and carbon monoxide, generate hydrogen and carbonic acid gas, this is component more than, the gas solid catalytic reaction system of many reactions, reactional equation is: (1) CH
3oH → CO+2H
2, (2) H
2o+CO → CO
2+ H
2, (3) CH
3oH+H
2o → CO
2+ 3H
2, the H that reforming reaction generates
2and CO
2, reformer chamber is connected by connecting pipeline with hydrogen purification apparatus, and all or part of of connecting pipeline is arranged at reformer chamber, and the high temperature by reformer chamber continues the gas that heating exports from reformer chamber, described connecting pipeline is as the buffering between reformer chamber and hydrogen purification apparatus, make the temperature of the gas exported from reformer chamber identical with the temperature of hydrogen purification apparatus or close, obtain hydrogen from the aerogenesis end of hydrogen purification apparatus, be supplied to petroleum products hydrofining system 4.The utility model respectively organizes the mode that methanol-water reformation hydrogen production module adopts reformer reformation hydrogen production at the temperature of 300-570 DEG C and under catalyst action, its hydrogen manufacturing speed and efficiency high, methanol-water feedstock conversion efficiency and utilization ratio high, good stability; Because the temperature of hydrogen purification apparatus is identical with reformer chamber temperature or close, therefore, hydrogen purification efficiency can be significantly improved and reduce hydrogen purification difficulty, realizing fast film and be separated.
Described methanol-water reformation hydrogen production module 3 comprises two kinds of preferred structure modes:
As shown in Figure 4, the preferred structure mode of the first methanol-water reformation hydrogen production module 3 is: described methanol-water reformation hydrogen production module 3 is integrated with interchanger 33, described interchanger 33 is installed on the transport pipe between methanol-water Storing and conveying device 2 and reformer 31, the first alcohol and water raw material of low temperature is in interchanger 33, the high-temperature gas exported with reformer chamber 31 carries out heat exchange, and first alcohol and water material temperature raises, vaporization; Described reformer 31 is provided with electric heater 313, and this electric heater 313 provides 300-570 DEG C of temperature for reformer chamber 311; The hydrogen of the aerogenesis end output of described hydrogen purification apparatus 312, after interchanger 33, temperature reduces, then is supplied to petroleum products hydrofining system 4.
Further, be also provided with between described interchanger 33 and reformer 31 and compensate vapourizing unit 34, this compensation vapourizing unit 34 is provided with electric heater 341, and described first alcohol and water raw material can be vaporized further after compensating vapourizing unit 34.
As shown in Figure 5, the preferred structure mode of the second methanol-water reformation hydrogen production module 3 is: described methanol-water reformation hydrogen production module 3 is integrated with interchanger 35, described interchanger 35 is installed on the transport pipe between methanol-water Storing and conveying device 2 and reformer 321, the first alcohol and water raw material of low temperature is in interchanger 35, the high-temperature gas exported with reformer chamber 321 carries out heat exchange, and first alcohol and water material temperature raises, vaporization; Vaporizing chamber (not shown) is not also had in described reformer 32, described first alcohol and water raw material enters vaporizing chamber vaporization in interchanger after 35 heat exchange, methanol steam after vaporization and water vapor enter reformer chamber 321, reformer chamber 321 bottom and middle portion temperature are 300-420 DEG C, and the temperature on reformer chamber 321 top is 400-570 DEG C; The all or part of top being arranged at reformer chamber of the connecting pipeline between described reformer chamber 321 and hydrogen purification apparatus 322; The hydrogen of the aerogenesis end output of described hydrogen purification apparatus 322, after interchanger 35, temperature reduces, then is supplied to petroleum products hydrofining system 4.
Further, as shown in Figure 5-Figure 8, described reformer 32 one end is provided with starter gear 5, and this starter gear 5 comprises cup 51, cup 51 is provided with raw material input channel 52, heating and gasifying pipeline 53, portfire 54 and temperature detection device 55; Described raw material input channel 52 can input first alcohol and water raw material, and raw material input channel 52 is connected with heating and gasifying pipeline 53, and first alcohol and water raw material enters after heating and gasifying pipeline 53 through raw material input channel 52, exports from the end of heating and gasifying pipeline 53; The position of described portfire 54 is corresponding with the end of heating and gasifying pipeline 53, for lighting a fire to the first alcohol and water raw material exported in heating and gasifying pipeline 53, first alcohol and water raw material is through portfire 54 ignition, combustion, can heat heating and gasifying pipeline 53, make the first alcohol and water material gasification in heating and gasifying pipeline 53 and strengthen rapidly intensity of combustion, and then heating for reformer 32; Described temperature detection device 55 is for detecting the other temperature of heating and gasifying pipeline 53; After described reformer 32 starts hydrogen manufacturing, the hydrogen partial that reformer 32 is obtained is or/and residual air is run by burning maintenance reformer 32.Reformer 32 utilizes starter gear 5 to heat for reformer 32 just, just makes reformer 32 start, and then reforming reaction occurs, and start time can complete in 5 minutes, and very fast, after having started, starter gear 5 cuts out.
As Figure 6-Figure 8, described cup 51 comprises the liquid containing portion 512 above installation portion 511 and installation portion, described raw material input channel 52, heating and gasifying pipeline 53, portfire 54 and temperature detection device 55 are all installed on the installation portion 511 of cup, described liquid containing portion 512 can hold the first alcohol and water raw material exported from heating and gasifying pipeline 53 end, and described liquid containing portion 512 upper end is also provided with liquid Splashproof cover 513.After raw material input channel 52 inputs first alcohol and water raw material, when heating and gasifying pipeline 53 exports, unnecessary first alcohol and water raw material can be contained in the liquid containing portion 512 of cup, certainly, after first alcohol and water raw material burns rapidly, the first alcohol and water raw material in liquid containing portion 512 also can gasification, and combustion.Described liquid Splashproof cover 513 can prevent the first alcohol and water raw material splashes when gasification, and combustion in liquid containing portion 512.Described heating and gasifying pipeline 53 comprises straight-through pipeline section 531, pigtail 532 and upper arch pipeline section 533 successively, described first alcohol and water raw material can after straight-through pipeline section 531 rises to extreme higher position, decline through pigtail 532 spiral again, then export after upper arch pipeline section 533.Like this, when starter gear 5 is started working, first alcohol and water raw material enters heating and gasifying pipeline 53, and first alcohol and water raw material is under the effect of upper arch pipeline section 533, first alcohol and water raw material can ooze, so that portfire is lighted a fire from the end of upper arch pipeline section 533 in the mode of drippage; After lighting a fire successfully, because the entire length of pigtail 532 is long, heating surface area is large, and therefore, the first alcohol and water raw material in pigtail 532 can fully by thermal evaporation.
As Figure 6-Figure 8, the bottom side of described cup 51 is provided with air intake cover plate 56, this air intake cover plate is provided with air channel 561, outside air can enter in reformer 32 through this air channel, the outside air entered from this air channel 561 can be starter gear 5 provides oxygen, also can be reformer 32 and oxygen is provided, for improving air inlet, fan (not shown) can be increased outside air channel 561; Described raw material input channel 52 is provided with magnetic valve, opens or closes to control raw material input channel 52.Described portfire can adopt resistant to elevated temperatures lighter for ignition on market, such as polarity formula pulse type ignitor etc.
In technique scheme, described hydrogen purification apparatus 312 or 322 is membrane separation unit, and this membrane separation unit is the membrane separation unit at porous ceramic surface Vacuum Deposition palladium-silver alloy, and coatings is palladium-silver alloy, the mass percent palladium of palladium-silver alloy accounts for 75%-78%, and silver accounts for 22%-25%.The manufacturing process of membrane separation unit can refer to the patent of invention 201210563913.5 that the applicant Shanghai Hejide Dynamic Hydrogen Machine Co., Ltd. applied on December 21st, 2012, membrane separation apparatus of methanol-water hydrogen producer and preparation method thereof.
For the production technique of petroleum products hydrorefined hydrogen raw material production equipment, comprise the following steps:
(1) petroleum products hydrofining system is in the process of hydrofining reaction, and instant hydrogen raw materials requirement amount is fed back to control device;
(2) control device operates according to the methanol-water reformation hydrogen production module of instant hydrogen raw materials requirement amount information Control proper amt, and controls the methanol-water reformation hydrogen production module conveying first alcohol and water raw material of methanol-water Storing and conveying device to running; When instant hydrogen raw materials requirement amount is less, control less methanol-water reformation hydrogen production module running, when instant hydrogen raw materials requirement amount is larger, control more methanol-water reformation hydrogen production module running;
(3) the work operational situation of each group methanol-water reformation hydrogen production module of control device detecting real-time, when any one group of methanol-water reformation hydrogen production module running is abnormal, the methanol-water reformation hydrogen production module that control device controls this exception shuts down, and control the methanol-water reformation hydrogen production module running that is in holding state, or the methanol-water reformation hydrogen production module controlled in other runnings accelerates hydrogen manufacturing speed, shut down with the methanol-water reformation hydrogen production module compensated because of this exception and the hydrogen manufacturing amount that reduces.
The above is only the utility model better embodiment, every above embodiment is done according to the technical solution of the utility model any trickle amendment, equivalent variations and modification, all belong in the scope of technical solutions of the utility model.
Claims (9)
1. one kind for petroleum products hydrorefined hydrogen raw material production equipment, it is characterized in that: comprise control device, methanol-water Storing and conveying device and at least three group methanol-water reformation hydrogen production modules, described control device and methanol-water Storing and conveying device and each organize methanol-water reformation hydrogen production module and be all electrically connected, to control the working order of methanol-water Storing and conveying device and each group methanol-water reformation hydrogen production module; The hydrogen that described each group of methanol-water reformation hydrogen production module obtains directly sends petroleum products hydrofining system to by transport pipe, this petroleum products hydrofining system is in hydrorefined process, instant hydrogen raw materials requirement amount is fed back to control device, this control device operates according to the methanol-water reformation hydrogen production module of the hydrogen raw materials requirement amount information Control proper amt of petroleum products hydrofining system, and controls the methanol-water reformation hydrogen production module conveying first alcohol and water raw material of methanol-water Storing and conveying device to running.
2. according to claim 1 for petroleum products hydrorefined hydrogen raw material production equipment, it is characterized in that: described methanol-water Storing and conveying device comprises methanol-water storage vessel and transferpump, store liquid first alcohol and water raw material in described methanol-water storage vessel, described transferpump is used for the first alcohol and water feedstock transportation in methanol-water storage vessel to methanol-water reformation hydrogen production module; The quantity of described transferpump and the quantity of methanol-water reformation hydrogen production module match, and the quantity of described methanol-water storage vessel is equal to or less than the quantity of transferpump.
3. according to claim 1 for petroleum products hydrorefined hydrogen raw material production equipment, it is characterized in that: described methanol-water reformation hydrogen production module comprises reformer, reformer chamber and hydrogen purification apparatus is provided with in this reformer, the temperature of reformer chamber is 300-570 DEG C of temperature, reformer chamber is provided with catalyzer, first alcohol and water is at the obtained hydrogen-containing gas of reformation hydrogen production reaction of reformer chamber generation first alcohol and water, reformer chamber is connected by connecting pipeline with hydrogen purification apparatus, the all or part of of connecting pipeline is arranged at reformer chamber, high temperature by reformer chamber continues the gas that heating exports from reformer chamber, described connecting pipeline is as the buffering between reformer chamber and hydrogen purification apparatus, make the temperature of the gas exported from reformer chamber identical with the temperature of hydrogen purification apparatus or close, obtain hydrogen from the aerogenesis end of hydrogen purification apparatus, be supplied to petroleum products hydrofining system.
4. according to claim 3 for petroleum products hydrorefined hydrogen raw material production equipment, it is characterized in that: described methanol-water reformation hydrogen production module is integrated with interchanger, described interchanger is installed on the transport pipe between methanol-water Storing and conveying device and reformer, the first alcohol and water raw material of low temperature is in interchanger, the high-temperature gas exported with reformer chamber carries out heat exchange, and first alcohol and water material temperature raises, vaporization; Described reformer is provided with electric heater, and this electric heater provides 300-570 DEG C of temperature for reformer chamber; The hydrogen of the aerogenesis end output of described hydrogen purification apparatus, after interchanger, temperature reduces, then is supplied to petroleum products hydrofining system.
5. according to claim 4 for petroleum products hydrorefined hydrogen raw material production equipment, it is characterized in that: between described interchanger and reformer, be also provided with compensation vapourizing unit, this compensation vapourizing unit is provided with electric heater, and described first alcohol and water raw material can be vaporized further after compensating vapourizing unit.
6. according to claim 3 for petroleum products hydrorefined hydrogen raw material production equipment, it is characterized in that: described methanol-water reformation hydrogen production module is integrated with interchanger, described interchanger is installed on the transport pipe between methanol-water Storing and conveying device and reformer, the first alcohol and water raw material of low temperature is in interchanger, the high-temperature gas exported with reformer chamber carries out heat exchange, and first alcohol and water material temperature raises, vaporization; Also vaporizing chamber is not had in described reformer, described first alcohol and water raw material enters vaporizing chamber vaporization in interchanger after heat exchange, methanol steam after vaporization and water vapor enter reformer chamber, and reformer chamber bottom and middle portion temperature are 300-420 DEG C, and the temperature on reformer chamber top is 400-570 DEG C; The all or part of top being arranged at reformer chamber of the connecting pipeline between described reformer chamber and hydrogen purification apparatus; The hydrogen of the aerogenesis end output of described hydrogen purification apparatus, after interchanger, temperature reduces, then is supplied to petroleum products hydrofining system.
7. according to claim 6 for petroleum products hydrorefined hydrogen raw material production equipment, it is characterized in that: described reformer one end is provided with starter gear, this starter gear comprises cup, cup is provided with raw material input channel, heating and gasifying pipeline, portfire and temperature detection device; Described raw material input channel can input first alcohol and water raw material, and raw material input channel is connected with heating and gasifying pipeline, and first alcohol and water raw material enters after heating and gasifying pipeline through raw material input channel, exports from the end of heating and gasifying pipeline; The position of described portfire is corresponding with the end of heating and gasifying pipeline, for lighting a fire to the first alcohol and water raw material exported in heating and gasifying pipeline, first alcohol and water raw material is through ignition device afterfire, can heat heating and gasifying pipeline, make heating and gasifying ducted first alcohol and water material gasification and strengthen rapidly intensity of combustion, and then being reformer heating; Described temperature detection device is for detecting the other temperature of heating and gasifying pipeline; After described reformer starts hydrogen manufacturing, the hydrogen partial that reformer is obtained is or/and residual air is run by burning maintenance reformer.
8. according to claim 7 for petroleum products hydrorefined hydrogen raw material production equipment, it is characterized in that: described cup comprises the liquid containing portion above installation portion and installation portion, described raw material input channel, heating and gasifying pipeline, portfire and temperature detection device are all installed on the installation portion of cup, described liquid containing portion can hold the first alcohol and water raw material exported from heating and gasifying pipe end, and described liquid containing portion upper end is also provided with liquid Splashproof cover; Described heating and gasifying pipeline comprises straight-through pipeline section, pigtail and upper arch pipeline section successively, and described first alcohol and water raw material after straight-through pipeline section rises to extreme higher position, then can decline through pigtail spiral, then exports after upper arch pipeline section; The bottom side of described cup is provided with air intake cover plate, and this air intake cover plate is provided with air channel, and outside air can enter in reformer through this air channel; Described raw material input channel is provided with magnetic valve, opens or closes to control raw material input channel.
9. according in claim 3 ~ 8 described in any one for petroleum products hydrorefined hydrogen raw material production equipment, it is characterized in that: described hydrogen purification apparatus is membrane separation unit, this membrane separation unit is the membrane separation unit at porous ceramic surface Vacuum Deposition palladium-silver alloy, and coatings is palladium-silver alloy.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104743512A (en) * | 2015-04-16 | 2015-07-01 | 广东合即得能源科技有限公司 | Equipment and process for producing crude hydrogen for hydrogenizing and refining petroleum product |
| JP2020125798A (en) * | 2019-02-04 | 2020-08-20 | 住友金属鉱山株式会社 | Methanol delivery pipe support member |
-
2015
- 2015-04-16 CN CN201520229923.4U patent/CN204643834U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104743512A (en) * | 2015-04-16 | 2015-07-01 | 广东合即得能源科技有限公司 | Equipment and process for producing crude hydrogen for hydrogenizing and refining petroleum product |
| JP2020125798A (en) * | 2019-02-04 | 2020-08-20 | 住友金属鉱山株式会社 | Methanol delivery pipe support member |
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