CN1049873C - Technology for preparing hydrogen by mixing dry gas and light oil of refinery - Google Patents
Technology for preparing hydrogen by mixing dry gas and light oil of refinery Download PDFInfo
- Publication number
- CN1049873C CN1049873C CN96122320A CN96122320A CN1049873C CN 1049873 C CN1049873 C CN 1049873C CN 96122320 A CN96122320 A CN 96122320A CN 96122320 A CN96122320 A CN 96122320A CN 1049873 C CN1049873 C CN 1049873C
- Authority
- CN
- China
- Prior art keywords
- dry gas
- gas
- hydrogen
- mixing
- light oil
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/32—Hydrogen storage
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to the technology for preparing hydrogen by mixing refinery dry gas and white oil, which belongs to the refining of mixtures containing hydrocarbon. The present invention is characterized in that the mixed-phase feeding of refinery dry gas with high hydrogen content and without alkene or nitrogen or other kinds of mixed gas and the white oil is used, a process flow orderly comprises gas-phase mixing, ethanolamine desulfurization, liquid separation, pressure boost, gas-liquid phase mixing, heating, cobalt-molybdenum and zinc oxide desulfurization, and hydrogen of which the purity is higher than 98% can be obtained by a converter. Dry air quantity can be arbitrarily selected from the range of 0 to 100 wt% in the mixed-phase feeding. The present invention simplifies flow paths and equipment without needing a circulation oil separation flow path and the replenishment of external hydrogen gas, the cost of the hydrogen gas is reduced by 28 to 32%, and energy consumption is reduced by 7 to 8%. The present invention has the advantage of no secondary pollution.
Description
The present invention relates to oil refinery dry gas and light oil technology for preparing hydrogen by mixing, belong to the refining of hydrocarbon-containing mixture.
The refinery hydrogen preparing technology of prior art light oil commonly used is made raw material, and also useful oil field gas, Sweet natural gas or rich tail gas of coking plant are made raw material.CN92111165.7 patent disclosure " oil refinery dry gas and the charging of petroleum naphtha mixed phase, the method for producing hydrogen, methane, carbon monoxide, carbonic acid gas through hydrofining ", this technology utilizes hydrogeneous 18-30% (v), to contain alkene 10-20% (v), nitrogenous 5-8% (oil refinery dry gas v), remove wherein hydrogen sulfide, carbon monoxide, carbonic acid gas through diethanolamine, again through gas-liquid separation; Oil refinery dry gas after the separation is compressed to boost, and with the charging of petroleum naphtha mixed phase, through hydrofining, desulfurization, deep refining, makes the hydrocarbon flow behind the mixed phase become the steam reforming charging; Generate hydrogen, methane, carbon monoxide, carbonic acid gas through conversion reaction.Oil refinery dry gas is regulated in the 20-80% of mixed phase charging (w) scope.
Olefin(e) centent height in the dry gas that the refinery hydrogen preparing technology of prior art is adopted need be provided with circulation and dividing oily flow process to reduce concentration of olefin in the raw material, makes that technical process is long, complicated operation; Hydrogen richness is low in the dry gas, need add external hydrogen in hydrogenation reaction; Nitrogen content height in the dry gas can not be produced highly purified industrial hydrogen; And adopt the sodium hydroxide washing because of H2S content is high, have sodium sulphite to produce, cause secondary pollution.
The present invention is intended to overcome the shortcoming of prior art and a kind of oil refinery dry gas and light oil technology for preparing hydrogen by mixing is provided.
The object of the present invention is achieved like this: see accompanying drawing.Adopt hydrogen richness height, the oil refinery dry gas that does not contain alkene and nitrogen or its gas mixture and the charging of light oil mixed phase, just can simplify technical process, make highly purified hydrogen.Its technical process is: hydrogeneous 30-85% (v), do not contain the oil refinery dry gas of alkene and nitrogen or its gas mixture (7), (8), (9) enter mixing tank (1), control pressure 0.8-1.2MPa enters thanomin thionizer (2); In thionizer (2), dry gas flows from bottom to top, and reverse contact of diethyl Propanolamine (10) with getting off from cat head reduced to below the 20ppm H2S concentration in the dry gas; The dry gas that comes out from thionizer (2) is behind a minute flow container (3), enter residue gas compressor (4), through being forced into 1.8-2.6MPa, the light oil (12) that comes out with raw oil pump is mixed into raw materials furnace and heating (5), raw material is heated to 330-380 ℃, steam/hydrocarbons ratio 4.0-5.0, enters cobalt molybdenum and zinc oxide desulfurization reactor (6); The first half dress hydrogenation catalyst (T201) of reactor (6), Lower Half dress Zinc oxide desulfurizer (T306) carries out hydrogenation reaction earlier in reactor (6), the organosulfur in the raw material is become inorganic sulfur, and then, make its sulphur content less than 0.2ppm through oxidation sweetening; Enter converter (steam conversion catalyst Z402/Z405) (13) at last and produce hydrogen.In the accompanying drawing, (11) are that rich gas goes regeneration.
Said hydrogeneous 30-85% (v), does not contain the oil refinery dry gas of alkene and nitrogen or its gas mixture (7), (8), (9), can be hydrocracking dry gas (7), the gas mixture of hydrocracking dry gas (7) and hydrofining dry gas (8) also can be the gas mixture of hydrocracking dry gas (7), hydrofining dry gas (8) and distillation dry gas (9).
Said light oil (12) can be light naphthar, heavy naphtha, raffinate oil or liquid hydrocarbon.
In the mixed phase air inlet, dry gas or its air-fuel mixture amount can be selected arbitrarily from 0-100% (w).Promptly can separate independent hydrogen manufacturing with light oil (12) with dry gas or its gas mixture (7), (8), (9), also can be with dry gas or its gas mixture (7), (8), (9) and light oil (12) with the hydrogen manufacturing of arbitrary proportion mixed phase.
Adopt oil refinery dry gas of the present invention and light oil technology for preparing hydrogen by mixing, the hydrocracking dry gas of refinery, hydrofining dry gas and distillation dry gas obtain to make full use of, and make hydrogen cost decline 28-32%, and plant energy consumption reduces 7-8%; Can make dry gas and light oil separate independent hydrogen manufacturing, also available dry gas and light oil are with the hydrogen manufacturing of arbitrary proportion mixed phase, and batching is flexible, and smooth operation makes industrial hydrogen purity and is higher than 98%; Technical process is simplified, and does not need circulation to divide an oily flow process, does not need to introduce external hydrogen and replenishes, and has reduced by 7 equipment than the technical process of prior art, thereby has reduced investment, has simplified operation; It is low that the dry gas of charging contains H2S, do not need the sodium hydroxide alkali cleaning, do not have sodium sulphite to produce, thereby avoided secondary pollution; The nonnitrogenous gas of the dry gas of charging does not corrode rear portion equipment, especially can prolong the work-ing life of converting furnace; The charging dry gas does not contain alkene, and conversion catalyst is difficult for knot carbon, has prolonged the work-ing life of conversion catalyst greatly, thereby has prolonged the production cycle of device.
Accompanying drawing is oil refinery dry gas of the present invention and light oil technology for preparing hydrogen by mixing schema.
Below in conjunction with embodiment technical scheme of the present invention is done further statement.
Embodiment 1
Adopt hydrocracking dry gas and light oil preparing hydrogen by mixing.Dry gas: light oil (w)=5.0: 0.5-5.5: 1.0, under dry gas pressure 0.8-1.2MPa, compressor delivery pressure 1.8-2.6MPa, 330-380 ℃ of furnace outlet temperature, steam/hydrocarbons ratio 4.0-5.0 condition, sulphur content makes purity at last and is higher than 98% industrial hydrogen less than 0.2ppm after the desulfurization.
Adopt the hydrocracking dry gas hydrogen manufacturing separately.Under dry gas pressure 1.0-1.2MPa, compressor delivery pressure 2.0-2.6MPa, 350-380 ℃ of furnace outlet temperature, the steam/hydrocarbons ratio 4.0-4.8 condition, sulphur content makes purity at last and is higher than 98% industrial hydrogen less than 0.2PPm after the desulfurization.
Adopt the gas mixture (by 3: 1-4: 2 mix) and light oil preparing hydrogen by mixing of hydrocracking dry gas and hydrofining dry gas.Dry gas: light oil (w)=5.5: 0.8-5.6: 1.0, under dry gas pressure 0.9-1.2MPa, compressor delivery pressure 2.1-2.6MPa, 360-380 ℃ of furnace outlet temperature, steam/hydrocarbons ratio 4.0-4.9 condition, sulphur content makes purity at last and is higher than 98% industrial hydrogen less than 0.2ppm after the desulfurization.
Embodiment 4
Adopt the gas mixture (by 3: 1: 0.5-4: mix at 2: 1) and light oil preparing hydrogen by mixing of hydrocracking dry gas, hydrofining dry gas and distillation dry gas.Dry gas: light oil (w)=6.0: 1.0-6.5: 1.2, under the condition of dry gas pressure 1.1-1.2MPa, compressor delivery pressure 2.2-2.6MPa, 350-380 ℃ of furnace outlet temperature, steam/hydrocarbons ratio 4.0-4.7, sulphur content makes purity and is higher than 98% industrial hydrogen less than 0.2ppm after the desulfurization.
Adopt gas mixture (by 3: 1: the 0.5) hydrogen manufacturing separately of hydrocracking dry gas, hydrofining dry gas and distillation dry gas, 340-370 ℃ of dry gas pressure 0.8-1.1MPa, compressor delivery pressure 2.0-2.4MPa, furnace outlet temperature, under the condition of steam/hydrocarbons ratio 4.0-4.6, sulphur content makes purity and is higher than 98% industrial hydrogen less than 0.2ppm after the desulfurization.
Claims (5)
1. oil refinery dry gas and light oil technology for preparing hydrogen by mixing, (v), oil refinery dry gas (7), (8), (9) that do not contain alkene and nitrogen enter mixing tank (1) to it is characterized in that adopting hydrogen richness 30-85%, control pressure 0.8-1.2Mpa, enter thanomin thionizer (2), in thionizer (2), dry gas flows from the bottom up, and reverse contact of diethyl Propanolamine (10) with getting off from cat head makes H in the dry gas
2S concentration is reduced to below the 20PPm; The dry gas that comes out from thionizer (2) is behind a minute flow container (3), enter residue gas compressor (4), through being forced into 1.8-2.6Mpa, the light oil (12) that comes out with raw oil pump is mixed into raw materials furnace and heating (5), raw material is heated to 330-380 ℃, steam/hydrocarbons ratio 4.0-5.0, enter cobalt molybdenum and zinc oxide desulfurization reactor (6), the first half dress hydrogenation catalyst of reactor (6), Lower Half dress Zinc oxide desulfurizer carries out hydrogenation reaction earlier in reactor (6), organosulfur in the raw material is become inorganic sulfur, and then, making its sulphur content less than 0.2ppm through zinc oxide desulfurization, the most laggard converter (steam reforming catalysts) (13) is produced hydrogen.
2. by described oil refinery dry gas of claim 1 and light oil technology for preparing hydrogen by mixing, it is characterized in that (v), oil refinery dry gas (7), (8), (9) that do not contain alkene and nitrogen are hydrocracking dry gas (7) to said hydrogeneous 30-85%.
3. by described oil refinery dry gas of claim 1 and light oil technology for preparing hydrogen by mixing, it is characterized in that (v), oil refinery dry gas (7), (8), (9) that do not contain alkene and nitrogen are that hydrocracking dry gas (7) and hydrofining dry gas (8) press 3: 1-4: 2 blended gas mixtures to said hydrogeneous 30-85%.
4. by described oil refinery dry gas of claim 1 and light oil technology for preparing hydrogen by mixing, it is characterized in that (v), oil refinery dry gas (7), (8), (9) that do not contain alkene and nitrogen are that hydrocracking dry gas (7) and hydrofining dry gas (8), distillation dry gas (9) were pressed 3: 1: 0.5-4: 2: 1 blended gas mixtures to said hydrogeneous 30-85%.
5. by claim 1,2,3 or 4 described oil refinery dry gas and light oil technology for preparing hydrogen by mixing, it is characterized in that in parallel feeding that dry gas or its gas mixture are selected arbitrarily from 0-100% (w).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96122320A CN1049873C (en) | 1996-10-21 | 1996-10-21 | Technology for preparing hydrogen by mixing dry gas and light oil of refinery |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96122320A CN1049873C (en) | 1996-10-21 | 1996-10-21 | Technology for preparing hydrogen by mixing dry gas and light oil of refinery |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1180657A CN1180657A (en) | 1998-05-06 |
| CN1049873C true CN1049873C (en) | 2000-03-01 |
Family
ID=5127260
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN96122320A Expired - Fee Related CN1049873C (en) | 1996-10-21 | 1996-10-21 | Technology for preparing hydrogen by mixing dry gas and light oil of refinery |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1049873C (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9302910B2 (en) | 2008-10-24 | 2016-04-05 | Shanghai Huachang Environment Protection Co., Ltd. | Short-flow process for desulfurization of circulating hydrogen and device for the same |
| CN101434381B (en) * | 2008-10-24 | 2011-07-13 | 上海华畅环保设备发展有限公司 | Short process flow recycle hydrogen desulfuration method and apparatus |
| CN105586088B (en) * | 2014-10-23 | 2017-10-20 | 中国石油化工股份有限公司 | A kind of dry gas lime set processing method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE4210638A1 (en) * | 1991-09-12 | 1993-03-18 | Linde Ag | High purity hydrogen and carbon mon:oxide recovery from dry gas mixt. - by one stage partial condensation and purificn. giving high yield at reduced cost |
| CN1075740A (en) * | 1992-10-27 | 1993-09-01 | 中国石油化工总公司 | Oil refinery dry gas and the charging of petroleum naphtha mixed phase are produced hydrogen, methane, carbon monoxide, the method for carbonic acid gas from hydrofining |
-
1996
- 1996-10-21 CN CN96122320A patent/CN1049873C/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE4210638A1 (en) * | 1991-09-12 | 1993-03-18 | Linde Ag | High purity hydrogen and carbon mon:oxide recovery from dry gas mixt. - by one stage partial condensation and purificn. giving high yield at reduced cost |
| CN1075740A (en) * | 1992-10-27 | 1993-09-01 | 中国石油化工总公司 | Oil refinery dry gas and the charging of petroleum naphtha mixed phase are produced hydrogen, methane, carbon monoxide, the method for carbonic acid gas from hydrofining |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1180657A (en) | 1998-05-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100556997C (en) | A kind of method of utilizing coke(oven)gas to prepare synthetic natural gas | |
| CN101054538B (en) | Iron-base desulfurizer for catalyzing, translating and absorbing carbonyl sulfur at middle-low temperature and preparation thereof | |
| CN101676367B (en) | Improved hydrotreatment process | |
| CN101371967B (en) | Liquid gas sweetening alkali liquor oxidized regeneration method and apparatus | |
| AU2010357037A1 (en) | Process for converting biogas to a gas rich in methane | |
| CN103432902B (en) | The method of hydrodesulfurization tail gas clean-up recovering liquid hydrocarbon and NaHS | |
| CN103509598B (en) | A kind of hydrogenation system and method for producing ultra-low-sulphur diesel | |
| CN101418229B (en) | Mercaptans removal apparatus for light oil and mercaptans removal method thereof | |
| US7342145B2 (en) | Process for refining liquefied petroleum gas in a commercial scale | |
| CN106268219A (en) | A kind of iron oxide fine desulfurizer and preparation and application method thereof | |
| CN102703107A (en) | Method for manufacturing liquid hydrocarbon product with synthetic gas produced by biomass | |
| CN101319150B (en) | Hot-soda washing desulfurization method | |
| CN1049873C (en) | Technology for preparing hydrogen by mixing dry gas and light oil of refinery | |
| CN1055108C (en) | Preparation of hydrogen, methane, carbon monoxide, carbon dioxide by self-hydrogenation refining and mixed phase feeding of dry gas and naphtha from refining plant | |
| CN101469276B (en) | Oil-containing alkali liquor separation apparatus and method | |
| CN101434873A (en) | Producer gas desulphurization process | |
| CN102676251A (en) | Process for preparing methane by utilizing coke oven gas | |
| CN105731497B (en) | A kind of utilization sour gas produces the method and device of sodium acid carbonate | |
| CN1019663B (en) | Refining process for synthetic ammonia raw material gas | |
| CN108865253A (en) | The method of coal Direct Hydrogenation liquefaction richness production aromatic hydrocarbons | |
| CN109355098A (en) | A kind of low grade oils multi-stage conversion process | |
| CN107365599A (en) | A kind of food-grade normal hexane low-voltage hydrogenation production technology | |
| CN105727715B (en) | A kind of Acidic Gas Treating technique and system | |
| CN1660734A (en) | Method for producing methanol by using coke oven gas as raw material | |
| CN105731501B (en) | A kind of utilization sour gas produces the method and device of solid sodium bicarbonate |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |