CN1497039A - Process for preparing hydrocarbon product by synthetic gas using skeleton catalyst paste phase technology - Google Patents
Process for preparing hydrocarbon product by synthetic gas using skeleton catalyst paste phase technology Download PDFInfo
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- CN1497039A CN1497039A CNA2003101015275A CN200310101527A CN1497039A CN 1497039 A CN1497039 A CN 1497039A CN A2003101015275 A CNA2003101015275 A CN A2003101015275A CN 200310101527 A CN200310101527 A CN 200310101527A CN 1497039 A CN1497039 A CN 1497039A
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- 239000003054 catalyst Substances 0.000 title claims abstract description 171
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 49
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 49
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 45
- 238000004519 manufacturing process Methods 0.000 title abstract description 6
- 238000005516 engineering process Methods 0.000 title description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 146
- 239000002002 slurry Substances 0.000 claims abstract description 75
- 229910052742 iron Inorganic materials 0.000 claims abstract description 73
- 238000006243 chemical reaction Methods 0.000 claims abstract description 38
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 34
- 239000007788 liquid Substances 0.000 claims abstract description 34
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 34
- 239000002245 particle Substances 0.000 claims abstract description 24
- 239000000047 product Substances 0.000 claims description 79
- 238000000034 method Methods 0.000 claims description 72
- 230000008569 process Effects 0.000 claims description 65
- 239000007789 gas Substances 0.000 claims description 63
- 238000004062 sedimentation Methods 0.000 claims description 29
- 229910052739 hydrogen Inorganic materials 0.000 claims description 27
- 238000006555 catalytic reaction Methods 0.000 claims description 20
- 239000008187 granular material Substances 0.000 claims description 19
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 16
- 230000004913 activation Effects 0.000 claims description 16
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 15
- 239000001257 hydrogen Substances 0.000 claims description 15
- 238000001816 cooling Methods 0.000 claims description 14
- 238000000926 separation method Methods 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 239000012530 fluid Substances 0.000 claims description 9
- 239000006227 byproduct Substances 0.000 claims description 7
- 230000000694 effects Effects 0.000 claims description 7
- 229910052757 nitrogen Inorganic materials 0.000 claims description 7
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 4
- 238000001914 filtration Methods 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 3
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 2
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- 239000000725 suspension Substances 0.000 claims description 2
- 230000002779 inactivation Effects 0.000 claims 2
- 238000007701 flash-distillation Methods 0.000 claims 1
- 238000010924 continuous production Methods 0.000 abstract description 2
- 239000001993 wax Substances 0.000 description 49
- 239000012752 auxiliary agent Substances 0.000 description 22
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 18
- 239000012071 phase Substances 0.000 description 17
- 239000004411 aluminium Substances 0.000 description 16
- 229910052782 aluminium Inorganic materials 0.000 description 16
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 16
- 239000012429 reaction media Substances 0.000 description 14
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 13
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 13
- 229910052802 copper Inorganic materials 0.000 description 13
- 239000010949 copper Substances 0.000 description 13
- 229910052700 potassium Inorganic materials 0.000 description 13
- 239000011591 potassium Substances 0.000 description 13
- 239000002283 diesel fuel Substances 0.000 description 12
- 238000005194 fractionation Methods 0.000 description 12
- 239000003208 petroleum Substances 0.000 description 11
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 10
- 229910052748 manganese Inorganic materials 0.000 description 10
- 239000011572 manganese Substances 0.000 description 10
- 239000003245 coal Substances 0.000 description 8
- 239000003345 natural gas Substances 0.000 description 8
- 239000000203 mixture Substances 0.000 description 7
- 235000009508 confectionery Nutrition 0.000 description 6
- 239000000446 fuel Substances 0.000 description 6
- 230000005484 gravity Effects 0.000 description 6
- 239000000463 material Substances 0.000 description 6
- 229910052751 metal Inorganic materials 0.000 description 6
- 239000002184 metal Substances 0.000 description 6
- 239000000843 powder Substances 0.000 description 6
- 238000009835 boiling Methods 0.000 description 5
- 238000002360 preparation method Methods 0.000 description 5
- 230000009466 transformation Effects 0.000 description 5
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 4
- 229910045601 alloy Inorganic materials 0.000 description 4
- 239000000956 alloy Substances 0.000 description 4
- 235000013339 cereals Nutrition 0.000 description 4
- 238000013461 design Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 229920002472 Starch Polymers 0.000 description 3
- 230000001476 alcoholic effect Effects 0.000 description 3
- 239000012018 catalyst precursor Substances 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 3
- 239000012188 paraffin wax Substances 0.000 description 3
- 238000002203 pretreatment Methods 0.000 description 3
- 235000019698 starch Nutrition 0.000 description 3
- 241000196324 Embryophyta Species 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 239000012190 activator Substances 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000013467 fragmentation Methods 0.000 description 2
- 238000006062 fragmentation reaction Methods 0.000 description 2
- DCAYPVUWAIABOU-UHFFFAOYSA-N hexadecane Chemical compound CCCCCCCCCCCCCCCC DCAYPVUWAIABOU-UHFFFAOYSA-N 0.000 description 2
- 238000007689 inspection Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000011159 matrix material Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- KWYUFKZDYYNOTN-UHFFFAOYSA-M potassium hydroxide Inorganic materials [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 238000010791 quenching Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000000967 suction filtration Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 244000257039 Duranta repens Species 0.000 description 1
- 238000006424 Flood reaction Methods 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 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
- 238000005299 abrasion Methods 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 150000001298 alcohols Chemical class 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 238000005275 alloying Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 210000000988 bone and bone Anatomy 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000000975 co-precipitation Methods 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 239000007859 condensation product Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
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- 239000000706 filtrate Substances 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 229940057995 liquid paraffin Drugs 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 229910001092 metal group alloy Inorganic materials 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Substances [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 1
- 235000015320 potassium carbonate Nutrition 0.000 description 1
- CHWRSCGUEQEHOH-UHFFFAOYSA-N potassium oxide Chemical compound [O-2].[K+].[K+] CHWRSCGUEQEHOH-UHFFFAOYSA-N 0.000 description 1
- 229910001950 potassium oxide Inorganic materials 0.000 description 1
- YLLIGHVCTUPGEH-UHFFFAOYSA-M potassium;ethanol;hydroxide Chemical compound [OH-].[K+].CCO YLLIGHVCTUPGEH-UHFFFAOYSA-M 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 230000003449 preventive effect Effects 0.000 description 1
- 239000011164 primary particle Substances 0.000 description 1
- 239000010734 process oil Substances 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
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- 235000009566 rice Nutrition 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 230000001568 sexual effect Effects 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 238000009955 starching Methods 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
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- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 239000004711 α-olefin Substances 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Catalysts (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A continuous process is disclosed for the production of hydrocarbon liquids and wax by Fischer-Tropsch conversion of synthesis gas in contact with promoted skeletal iron catalyst particles in a slurry reactor. Wax product is readily separated from the skeletal iron catalyst in a catalyst settling drum and concentrated catalyst particles in wax slurry are recycled from the settling drum to the slurry reactor, while essentially solid-free wax is recovered as a product.
Description
Pertinent literature and application
This application be on March 27th, 2002 submit and just inspection phase series number be the follow-up of 10/107915 United States Patent (USP), wherein the latter is again to be the follow-up of 09/895621 United States Patent (USP) in the series number that submit and be in inspection phase July 2 calendar year 2001, and wherein the latter is again that the series number in application on September 21st, 1999 is that the 09/399852 present patent No. is the follow-up of 6277895 United States Patent (USP).
Invention field
The present invention relates to a kind of process that fossil energy is converted into liquid and gaseous hydrocarbons.Refer in particular to and fossil energy is converted into synthetic gas then synthetic gas to be converted into liquid fuel and wax or straight chain hydrocarbon be the process integration of primary product.Wherein the synthetic gas conversion reaction is mounted with saturated liquefied hydrocarbon one and is reaction medium and is suspended in wherein to contain or do not contain in the fine grain slurry attitude of the auxiliary agent skeletal iron catalyst phase reaction container and carries out.The most important thing is that catalyst solid particle easily autoreaction slurries is separated and reclaimed or be discarded.
Background of invention
The process that fossil energy such as coal, Sweet natural gas, refinery coke etc. are converted into liquid hydrocarbon fuel and/or chemical is the theme of whole industry member broad research and exploitation for many years always, attempt by this measure provide the real alternative orientation of crude production produce clean fuel especially high hexadecane value diesel oil and exploitation in the world the coal of maximum reserves as the competition raw material of basic hydrocarbon production.The existing considerable technological process that directly or indirectly fossil energy is converted into the liquefied hydrocarbon product has obtained exploitation, some bigger pilot plants have also been set up and have been moved, and have the commercial size factory of family more than 20 once to drop into the technology that coal conversion is a liquefied hydrocarbon approximately.More than 20 in the family, majority is being set up during the Second World War by German Government at this.These factories of half adopt well-known Fischer-Tropsch building-up process approximately, promptly by the contact process that generate liquid hydrocarbon of synthetic gas with catalyzer, are better in durante bello operation at that time at least.After this be exactly that Government of South Africa (SASOL) utilizes the indirect liquefaction process of fischer-tropsch reaction and iron catalyst successfully to set up the production equipment that a series of coals are converted into hydrocarbon fuel and chemical.What have that to be exactly the Shell Oil Co. build in Malaysia is the fixed bed Fischer-Tropsch synthesizer of raw material with cheap Sweet natural gas again.
From work angle, no matter the indirect liquefaction Fischer-Tropsch that coal matrix or Sweet natural gas set out synthesizes on engineering by good authentication.Yet, so far still distance is arranged by coal or the Sweet natural gas developer who carries out direct or indirect liquefaction process that sets out with economically success, be that directly or indirectly the higher running cost of liquefaction process also is a big reason in addition because the price of competition substitute crude oil is lower to a great extent.The economic operation of process depends on unstripped gas price, catalyzer cost and activity, abrasion resistance and other challenge significantly, and these restrictions obviously need be overcome or improve and reduce total process cost.Via Fischer-Tropsch synthetic coal or the potential in fact competition gap that can shorten this process and crude oil technology of Sweet natural gas base indirect liquefaction process.Key wherein is exactly to improve catalyst performance and the reactor design that is applied to be converted into by synthetic gas the Fischer-Tropsch building-up process of hydrocarbon product energetically.
The method that the hydrocarbon product of high value 1-alkene is rich in known a kind of preparation is, at first for example gasification or natural gas via steam reforming are converted into synthetic gas with fossil energy, be carbon monoxide and hydrogen, and then by the Fischer-Tropsch building-up process of using iron catalyst synthetic gas be converted into the liquefied hydrocarbon product again.But great majority are especially starched embrittlement easily in the attitude phase reactor, are broken for the superfine powder particle with the iron catalyst of precipitator method manufacturing under the popular response condition in the Fischer-Tropsch building-up process.Part in the synthetic product is a paraffin, the liquid phase reaction medium that forms in reactor has just become the slurries that are mixed with micron order granules of catalyst (quite a few is less than 1 micron), makes that the wax product after fischer-tropsch reaction becomes extremely difficult with separating of superfine granules of catalyst.So need separation means expensive and quite complexity to append in traditional Fischer-Tropsch synthesis process separating effect with the precipitated iron catalyst subparticle that improves Fischer-Tropsch synthetic and wherein carry secretly.The result is the loss of the precipitated iron catalyst that can be recycled and is attached to cost burden on the Fischer-Tropsch building-up process economy that wherein the latter is owing to replacing the loss catalyzer and granules of catalyst in the wax product being carried out isolating more multioperation cost cause.Obviously, the separation difficulty of catalyzer and wax product has become precipitated iron catalyst successful Application and business-like one big obstacle.
Do as a whole here and in the United States Patent (USP) 6265451 and 6277895 quoted, skeletal iron catalyst is used to produce the liquefied hydrocarbon product via the fossil origin synthetic gas in paste state bed reactor.In these patents explanation with proposed a kind of relative simplification and cheap method and can prepare the synthetic skeletal iron catalyst of Fischer-Tropsch, this catalyzer possess low wearing and tearing, with the separate easily performance of wax and synthetic gas transformation efficiency characteristics far above fused iron catalyst.And the unstripped gas transformation efficiency of this catalyzer is equivalent to the precipitated iron fischer-tropsch synthetic catalyst, and selectivity of product then stresses at fraction hydro carbons and a small amount of wax product.
Here we provide the invention of a complete process process, be successful land productivity advantage with skeletal iron catalyst in the slurry attitude phase reactor, and overcome narrated here by fossil energy for example the synthetic gas in Sweet natural gas or coal source produce the major limitation of the process of liquefied hydrocarbon.
Summary of the invention
A kind of synthetic gas is converted into the continuous catalysis process of hydrocarbon product, this process comprises the following steps:
The flow of feed gas that contains synthetic gas in reactor under the respective reaction condition contacts with skeletal iron catalyst particle in the slurry attitude bed, makes synthetic gas be converted into C
1-C
4Light hydrocarbon, C
5 +Product such as liquid hydrocarbon and wax,
Except the wax product, other product and by product are flowed out with vapour phase by reactor head, and are separated into gaseous by-products, light hydrocarbons gaseous product and C
5 +Liquefied hydrocarbon, the latter collects as primary product;
Draw the skeletal iron catalyst particulate slurry fluids that contains suspension by the overflow port of reactor and enter the catalyst sedimentation jar, the latter will be under the isolating condition that is suitable for granules of catalyst and wax, wherein said granules of catalyst can be deposited on described jar bottom after sedimentation, form the concentrated slurry of granules of catalyst and liquid wax;
Discharge the liquid wax that does not contain catalyzer substantially from described slurry tank top, bottom slurry tank, draw the slurries of enrichment granules of catalyst, pump into the circulation of reactor bottom as skeletal iron catalyst.
The successive processes that the synthetic gas that this invention provides is converted into the liquefied hydrocarbon product be by under certain operation condition in slurry attitude phase reactor material synthesis gas and be suspended in skeletal iron catalyst particle contact reacts in the liquid olefin medium, and then generate the C of gaseous by-products, low carbon number
1-C
4Hydro carbons and the C that comprises the wax product
5+The liquefied hydrocarbon product.Outside the paraffin removal product, above-mentioned product can flow out from reactor head, through the condensation refrigerated separation and collect C
5+Liquefied hydrocarbon is obtained petroleum naphtha and fraction of diesel oil through fractionation again, and gas-phase product can reclaim liquefied gas through handling, and also can remove by product CO
2Reclaim C later on
1, C
2, unconverted H
2And CO.Other has a slurries streamline to draw through the reactor overflow mouth from the main body reactor bed to enter catalyst settler, wherein become entrained in the base section that skeletal iron catalyst in the slurries just is concentrated in settling vessel, the latter mainly is granules of catalyst and a small amount of paraffin mixture of products.The separation of one waterpower rotary gas separator accelerator activator/wax before entering catalyst settler, also can be installed in slurries.Part after the relief outlet of settling vessel side is used for isolating catalyzer from the top discharging of settling vessel promptly reclaims the wax product.Sedimentation and the concentrated skeletal iron catalyst slurries that are enriched in settling vessel bottom then can return the main reactor bottom by the catalyst recirculation circuit.The catalyst concentration slurries that also will discharge some amount through the catalyst recirculation line are equivalent to the decaying catalyst of live catalyst additive with continuous discharge, thereby keep the catalyst activity sexual balance.
Reaction bed in the reactor of the present invention is formed by the liquid reaction medium that overflow line is kept above the cooling system top by including skeletal iron catalyst and built-in water cooler and liquid level.
The reactor operating temperature range is at 230 ℃-280 ℃, and pressure range is at 1.7-5.5MPa, and the air speed scope is at 1-5L/g-cat/hr.
The wax product is mainly collected by catalyst sedimentation separator side line, promptly discharges the back through side line and squeezes into filtration unit to remove the entrained catalyst of trace by pump.Filtered wax product enters a flash separator removing the light constituent that may carry, and reclaims product wax from the flasher bottom.
Skeletal iron catalyst is discharged the back and is experienced recycle circuit and squeezed into position below the cooling system of reactor by slush pump through settling vessel bottom.The suitable condition of catalyst sedimentation separator is 230-270 ℃ a temperature, the pressure of 1.5-5.0MPa and the 15-60 minute residence time.
What be applied to skeletal iron catalyst recommendation use of the present invention is that activatory contains the auxiliary agent catalyzer, although also can adopt the skeletal iron catalyst that does not contain auxiliary agent.This catalyzer will pass through hydrogen or/and nitrogen activates under heating condition before entering reaction process.
The skeletal iron catalyst of preferentially selecting for use comprises the iron of 50-90 (weight) %%, the copper of 0-5.0 (weight) %, the manganese of 0.1-5.0 (weight) %, the potassium of 0.1-3.0 (weight) % and the aluminium of residual content.Hydrocarbon product good selectivity, especially liquid fuel and alpha-olefin that this catalyzer has good catalyst strength and advantages of high catalytic activity and set out by CO and hydrogen.
The auxiliary agent skeletal iron catalyst that contains of the present invention adopts the preparation of improving one's methods, the metal block or the powder that are about to iron block or powder and non-ferrous components comprise that aluminium, copper, manganese mix, the heating of metal mixture makes it the metal alloy that fusion forms molten state, thereafter cool off this molten state alloy fast to room temperature (15-20 ℃), for example in water, quench etc., be to pulverize alloy so that tiny catalyst precursor alloying pellet to be provided afterwards, size range is at 0.1-10mm (10-10000 micron).By contacting the most of aluminium suction filtration in the alloy is fallen to form main body iron catalyst particle subsequently with alkaline solution.This main body iron catalyst is and then through supporting or impregnation steps forms the potassium loading of 0.1-3.0 (weight) %.Because use the rear catalyst ratio to be easier to separate by gravity settling and hydrocarbon product, this skeletal iron catalyst is suitable for starching attitude phase Fischer-Tropsch building-up process especially.
The accompanying drawing summary
Fig. 1 is detailed process flow figure, described use contain auxiliary agent or do not contain auxiliary agent skeletal iron catalyst and slurry attitude mutually fischer-tropsch reactor transform one way or the cyclical operation reaction process that synthetic gas is liquefied hydrocarbon and wax product.
Detailed description of the invention
Comprise the continuous process that wax separates
Referring to Fig. 1, this flow chart describes course of reaction of the present invention in detail, and preferential the employing contains the auxiliary agent bone The frame iron catalyst is in slurry attitude phase reactor. This process can be by once passing through or one-pass operation or synthesis gas is not anti-Should the partially recycled reactor that loops back. One-pass operation process formant among the present invention comprises: the gasification process device (101), catalyst activation tank (105), synthesis reactor (110), heat exchanger (115), catalyst sedimentation tank (120), Wax product flash vessel (125), reacting fluid flash evaporation tank (130) and cold flash tank (135), fractionating column (140) and fractionating column Top condenser (145), return tank (150) and reboiler (155).
With natural gas at upstream reformer or gasification installation to raw material of synthetic gas of the present invention (not shown in the diagram) Or coal is converted into synthesis gas. This synthesis gas is purified after removing sulphur and oxygen, as unstripped gas (201) by reactor Bottom inlet enters reactor (110), and by bottom distributor control flow. Stream keeps the catalyst powder in the slurries The end is suspended, thereby synthesis gas is converted into the liquid product of gaseous state and wide fraction. The reaction heat that produces is by cold But pipe (202) is removed, and imports boiling water in the cooling pipeline and produces steam.
Liquid level in the reactor remains on cooling tube by the ororrhea Flow Line (203) that flows to catalyst settler (120) On the line. Catalyst deposit in the slurries that (120) are discharged by reactor in catalyst settler is in the tank bottom, and The liquid that only contains a small amount of catalyst fines then Main Current to the top of tank. Carry secretly with dissolved gases and then leave sedimentation The vapour phase that tank is integrated with reactor top flows out line. The catalyst of 90-99% in the catalyst slurry that reactor is discharged To be deposited in the bottom of tank, remove from settling tank top and carry the liquid stream of seldom measuring catalyst fines secretly, and be subjected to liquid Face control is lower sends into filter (205) by pump (204), a small amount of catalyst fines is filtered remove. The cleaning filtrate then by Send into wax flash tank (125). Behind flash tank (125) discharge tail gas, clean wax product is then by pumping (206) and cooling (207) The recycling wax product.
The reactor slurry of discharging through (203) overflow line can be revolved through waterpower before entering catalyst sedimentation tank (120) Turn to separator (not shown in the diagram), the separation of accelerator activator/wax.
The major part of the concentrated slurry of catalyst sedimentation pot bottom is beaten by slush pump (208) and is looped back synthesis reactor (110). This liquid is concentrating for catalyst granules. Other has a small amount of slurries then to emit under flow-control (209). The slurry flow rate that loops back synthesis reactor (110) via settler (120) has been controlled synthesis reactor to catalysis The flooding velocity of agent settling tank. The level control that arranges at settling tank has just determined settling tank and synthetic reaction simultaneously The liquid level of device. The catalyst sedimentation tank is installed to certain height and just in time is higher than synthetic reaction to guarantee its liquid level The top of device cooling system (202).
The catalyst sedimentation tank is discharged and flowed under the influence of gravity into to the wax slurries by synthesis reactor continuously. Catalyst particles Grain sedimentation separation from the wax slurries is come and is enriched in the settling tank bottom. The wax product of being drawn by settling tank top contains The catalyst fines that is lower than 0.2 (weight) % is arranged. Fluid in the settling tank bottom then contains urging of 40 (weight) % that have an appointment Change the agent particle, these catalyst solids loop back in the reactor. The performance of slurries settling tank and preferred operations condition are total Tie as follows:
Conditional parameter slurries settling tank (120)
The position is vertical/high position
Temperature, ℃ 230-270
Pressure: MPaAbs 2.5-5.0
The time of staying, minute 15-60
Catalyst concn: % by weight
Clean wax product is less than 0.2 weight %
The about 40 weight % in slurry tank bottom
From synthesis reactor come out to enter the catalyst sedimentation jar liquid stream (203), overflow the wax liquid stream (204) that enters filtration unit and valve control be not set by the catalyst sedimentation jar by the catalyst concentration slurry fluids (208) that the circulation of catalyst sedimentation jar enters synthesis reactor.The top streamline of slurry tank and bottom streamline are carried by the variable-ratio positive-displacement pump, and the venturi flow table is all adopted in the flow demonstration on all these circuits.Flow through these pumps is controlled to regulate rate of pumping by the venturi flow table.Being difficult to of having taked that these preventive measures just can generate catalyst breakage drops to minimum from the possibility of the isolating fines of wax liquid.
The vapor phase product streamline that leaves reactor mainly comprises unreacted CO and H
2, add the CO that generates in the reaction
2, water, methane and boiling point be lower than the hydrocarbon product of wax.This reactor outlet fluid and boiler feed water heat exchange cooling (115) are to 150 ℃, and condensation product then enters separation column (140) behind flash tank (130).The steam that comes out from flash tank (130) gas phase and liquid phase after cooling off can be separated in cold separating tank (135), and wherein the liquefied hydrocarbon product just enters separation column (140).The overhead product that the fractionation of separation column (140) charging adopts method well known in the art to get off with condensation in the condenser (145) reclaims and causes.The product that fractionation is reclaimed is definite by design, for example, and C
5Product, C
6+Product, separation column tail G﹠W and alcohols etc.The wax product is then obtained from catalyst sedimentation fractionator (120).
Why process of the present invention can bring into play its effect is because unique skeletal iron catalyst is unlikely to as the easy fragmentation of co-precipitation iron catalyst, so catalyzer separates with wax liquid by gravity settling easily.
The catalyzer that is applied to this process preferentially selects for use one to contain the auxiliary agent skeletal iron catalyst, and it forms below narration to some extent.This catalyzer need carry out activation or preconditioning about 24 hours with the slurries form of liquid hydrocarbon medium formation in catalyst pretreatment jar (105) in hydrogen or nitrogen atmosphere and 250 to 350 ℃ of temperature ranges.Pretreated catalyzer is squeezed into reactor (110) by pump through bottom conduit (210) with the form of slurries.The catalyst concn of slurries is advisable with 20 (weight) % in reactor, and catalyst grain size is at the 30-100 micrometer range, and corresponding skeleton real density is 7.9 gram/cubic centimetres.
Under single-pass operation pattern of the present invention, flow to gas processing plant (101) through the cooling separator effluent air, in this device, reclaim liquefied gas (C
3-C
4), remaining gas can be used as exhaust emissions, uses or the gas that acts as a fuel for the downstream processing unit (plant).
Under cyclical operation pattern of the present invention, unreacted H in this synthesis tail gas
2Should give recovery with CO, and the recycled back synthesis reactor.
Though contain the skeletal iron catalyst of auxiliary agent is that process of the present invention is preferentially selected for use, and the skeletal iron catalyst that does not contain auxiliary agent also is suitable for this process.
Specificity of catalyst and preparation process
The present invention mainly provide a kind of have unique form contain the auxiliary agent skeletal iron catalyst effectively to be applied to through the Fischer-Tropsch building-up process by H
2Generate purpose liquid hydrocarbon product with the CO unstripped gas.This contains the auxiliary agent skeletal iron catalyst and contains the iron of 70-90 (weight) % and less than 10 (weight) % non-ferrous metal auxiliary agent, be mainly copper and manganese, and the potassium of 0.1-3.0 (weight) %, and all the other then are aluminium.The surface-area of this catalyzer is at 20-80m
2/ g scope is with 30-65m
2/ g is advisable, and size-grade distribution is at 10-10000 μ m.
This Preparation of catalysts process comprises: at first with iron block or powder and required non-ferrous metal piece or powder, here refer to aluminium, copper, manganese, press 20-80 (weight) % iron and 30-70 (weight) % non-ferrous metal components in proportions uniform mixing, typical mixture contains (weight): 35-55% iron, 40-60% aluminium, 1-15% manganese, 0-10% copper.This metal mixture forms a molten state alloy through being heated to, and the method for cooling off for example water quenching then fast is chilled to room temperature (15-20 ℃), and fragmentation obtains the catalyst precursor of granularity at 10-10000 μ m.This catalyst precursor particles then through the NaOH of 10-50% or the KOH aqueous solution 50-90 ℃ down and time enough for example under 20-150 minute the reactivity most aluminium suction filtration is fallen, being left is the basic framework iron catalyst.
Gained skeletal iron catalyst matrix then is transferred to suitable containing in the potassium alcoholic solution and floods, and alcoholic solvent is evaporated form the skeletal iron catalyst that supports 0.1-3 (weight) % potassium then.Wherein the alcoholic solution of Shi Yi potassium includes but not limited to: methanol-hydrogen potassium oxide, ethanol-potassium hydroxide or salt of wormwood.
Next contain the auxiliary agent skeletal iron catalyst activation or with processing, can be in fixed-bed reactor, 0.05-1.0NL/gcat/h, in hydrogen or the nitrogen gas stream, in 250-350 ℃, finish under the condition such as 2-12 hour, resulting activation contains auxiliary agent skeletal iron catalyst and a suitable medium for example whiteruss or ethanol activation and be transferred in the reactor stand-by.Other method is, this skeletal iron catalyst that contains auxiliary agent also can be at first with a reaction medium for example whiteruss mix and form slurries, and be transferred in the slurry attitude phase fischer-tropsch reactor directly and contain nitrogen with hydrogen and under conditions such as 0.3-3.0NL/gcat/h, 250-350 ℃ temperature, 2-24 hour, finish the activation or preconditioning process.At this moment, this skeletal iron catalyst promptly can be effectively applied to H
2With the CO unstripped gas through the Fischer-Tropsch building-up reactions with the process that generates the purpose hydrocarbon product.
The particle that contains the auxiliary agent skeletal iron catalyst that finally obtains is in the 10-10000 mu m range, and wherein the particle in the 1000-10000 scope is applicable to fixed-bed reactor, and small-particle scope 20-200 μ m then can be used for paste state bed reactor.
Contain the application of auxiliary agent skeletal iron catalyst in Fischer-Tropsch synthesis
The auxiliary agent skeletal iron catalyst that contains of the present invention is to containing CO and H
2Unstripped gas is extremely effective through the process that the Fischer-Tropsch building-up reactions generates required hydrocarbon product, especially for slurry attitude phase reactor.Effectively operation condition is: H
2/ CO mol ratio is 0.5-5: 1, catalyst weight concentration 5-40% (with respect to reaction medium whiteruss for example), fixed-bed reactor are used the 1-10mm grain graininess, slurry attitude phase reactor is adopted the granularity of 20-200 μ m, reaction pressure is at 1.0-3.0MPa, and the gas space velocity flow is 0.5-5.0NL/gcat/h.The slurries that heavy liquid hydrocarbon product such as wax and catalyst system therefor particle form in reactor can separate granules of catalyst fundamental sum wax product by gravity settling after drawing reactor.
The slurry attitude that application skeletal iron catalyst of the present invention is produced hydrocarbon product by synthetic gas is combined to can being illustrated by the following example of technological process, but is not limited to these embodiment.
Embodiment 1
1. H
2/ CO mol ratio is that 2.0 synthetic gas is a raw material, starches attitude in illustrated the present invention and is combined to and transforms in the Design of device to generate hydrocarbon product.The boiling point that reaction medium system reaction in the synthesis reactor generates is higher than about 400 ℃ heavy hydrocarbon product, and wherein suspending does not contain the skeletal iron catalyst of auxiliary agent.This catalyzer consists of iron 72.9 (weight) % and aluminium 27.1 (weight) %.Catalyst concn is 15 (weight) % in this reaction medium, and the primary particles diameter is the 44-74 micron, and specific surface area is 45 meters
2/ gram.
2. entering before the reactor, this catalyzer is used the hydrogen pre-treatment in fixed-bed reactor, and this catalyst activation condition is 350 ℃ of normal pressures, and hydrogen gas space velocity is 0.7NL/g-cat/hr, lasts 8 hours.
3. activate pretreated catalyzer and whiteruss furnishing slurries and send into reactor.The synthesis reactor operational condition is: pressure 2.5MPa, 270 ℃ of temperature, space velocity 1.5 mark rice
3/ kilogram-catalyzer/hour.Once by and under the loop-free condition, the CO transformation efficiency is 75 (mole) %, H
2Transformation efficiency is 36 (mole) %.Under the situation of stable operation, can obtain C
1-C
2Be 0.032 (kg/kg-catalyzer/hour), C
3-C
4Be 0.040 (kg/kg-catalyzer/hour), C
5+ hydrocarbon product is 0.106 (kg/kg-catalyzer/hour).But latter's fractionation is (weight %): petroleum naphtha (＜177 ℃) 54%, diesel oil 35%, wax 11%.
Embodiment 2
1. one starch attitude phase fischer-tropsch synthesizer designing treatment synthetic gas (H
2/ CO mol ratio is 2.0) and use and to contain the auxiliary agent skeletal iron catalyst, consist of (weight %) iron 86.9, aluminium 9.8, manganese 1.5, and copper 1.8.Reaction medium contains catalyzer 15 (weight) % in the reactor, and the initial particle scope is the 44-77 micron, 54 meters of specific surface areas
2/ gram.
2. with embodiment 1 step 2.
3. live catalyst activates with hydrogen in fixed-bed reactor earlier, and activation condition is 350 ℃ of normal pressures, and hydrogen gas space velocity is 0.7NM
3/ kg-cat/hr lasts 8 hours.Activation rear catalyst and liquid paraffin fraction are mixed into slurries, and deliver to the operation loss and the equilibrium activity of keeping catalyst reactor of synthesis reactor make-up catalyst under nitrogen protection continuously.The operational condition of synthesis reactor is: pressure 2.5MPa, 270 ℃ of temperature, space velocity 3.0NM
3/ kg-cat/hr.One way CO transformation efficiency is 78%, H
2Transformation efficiency is 33%.
4. the gaseous fluid of leaving from reactor head contains unconverted CO and H
2, C
1Above wide boiling range hydrocarbon product, and by product CO
2And H
2O etc.This streamline is separated into non-condensable gas and phlegma through the condensation cooling in the hot and cold separator.This non-condensable gas part is sent to gas treatment equipment to reclaim the liquefied gas portion C
3-C
4, remove CO
2, reclaim unconverted CO and H
2, and dry gas C
1And C
2The phlegma part then is pumped to separation column to obtain petroleum naphtha and fraction of diesel oil.
5. the reaction medium in the synthesis reactor is the heavy hydrocarbon product that generates in the process, and boiling point is higher than 380-400 ℃, wherein is suspended with granules of catalyst and forms slurries.Material synthesis gas is sent into by reactor bottom and is formed on the equally distributed countless rising bubbles of reactor cross section by the gas distribution facility, make the slurries in the total overall reaction volume be in full back-mixing state, thereby make the entire reaction bed temperature evenly and give good heat transfer between slurries and the inside reactor water cooler.
6. the inside reactor water cooler is a bundled tube, has enough surface-area and stablizes to keep temperature of reaction to draw the heat that building-up reactions was discharged.Boiler feed water circulation is arranged, draw heat and water vapour takes place in the cooling tube.Cooling tube all impregnated in the slurries bed, and the height of slurry attitude bed is controlled by overflow device, and heavy hydrocarbon product wax promptly with the form overflow of slurries to the catalyst sedimentation jar.Slurries stopped under 250 ℃ temperature 30-60 minute in slurry tank, then most of catalyst particle through gravity settling to a jar end.Only contain＜catalyst fines of 0.1 (weight) % from the effusive wax product of tank deck, obtain wax product after filtration.
7. under steady operation conditions, in this process, can obtain (kg/kg-catalyzer/time) C
1+ C
20.052, C
3+ C
40.072, C
5+ 0.208.The latter can obtain (weight %) through fractionation: petroleum naphtha 52%, diesel oil 42%, wax 6%.
8. successive reaction is after 100 hours, and catalyst particle size distributes following (weight %) in the reaction medium slurries: the 44-74 micron is 89%, and it is 1.2% that the 2.5-44 micron is 9.8%,＜2.5 microns.
Embodiment 3
1. H
2/ CO mol ratio is 0.7 synthetic gas, starches attitude in illustrated the present invention and is combined in the reaction unit design and is converted into hydrocarbon product.Adopt in the reactor to contain the auxiliary agent skeletal iron catalyst, it consists of (weight %): iron 90.4, aluminium 5.4, manganese 1.5, copper 1.8 and potassium 0.9.Initial particle size is the 44-77 micron, and specific surface area is 64 meters
2/ gram.Catalyst concn is 15 (weight) % in the reaction medium.
2. with embodiment 1 step 2.
3. with embodiment 2 steps 3, but one way CO transformation efficiency (mole %) is 82.5, H
2Transformation efficiency is 62.8.
4-6. step 4-6 with embodiment 2.
7. under steady operation conditions, can get following product (kg/kgcat/h): C1-C2 0.052, and C3-C4 0.079, C
5+0.208 the latter can get (weight %) through fractionation: petroleum naphtha 44, fraction of diesel oil 44, wax 12.
8. the gravity settling 15 minutes under 205 ℃ of temperature of the catalyst/wax slurries behind 500 hours continuous operation, the granules of catalyst of about 99 (weight) % is settled down to pot bottom, the wax liquid on jar top contains granules of catalyst＜0.1 (weight) %, catalyst particle size distribution following (weight) %:44-77 micron is 24.7% in the reaction medium, it is 5.3% that the 25-44 micron is 70.0%,＜2.5 microns.
Embodiment 4
1. She Ji slurry attitude is combined to the H of the material synthesis gas of reaction unit
2/ CO mol ratio is 1.23.Catalyst system therefor is formed (weight %): iron 90.6, aluminium 3.5, manganese 1.9, copper 3.2 and potassium 0.8.The catalyzer initial particle size is the 44-77 micron, and specific surface area is 58m2/g, and catalyst concn is 15 (weight) % in the reaction medium.
2. with the step 2 of embodiment 1.
3. with the step 3 of embodiment 2, but space velocity is 2.0NL/gcat/h, and per pass conversion (mole %) is CO68.9, H
238.1%.
4-6. step 4-6 with embodiment 2.
7. under steady operation conditions, can obtain following product (kg/kg-catalyzer/hour): C1-C2 0.043, and C3-C4 0.052, C
5+0.190; The latter can get (weight %) through fractionation: petroleum naphtha 53%, fraction of diesel oil 34% and wax 13%.
Embodiment 5
1. She Ji slurry attitude is combined to the H of the material synthesis gas of reaction unit
2/ CO mol ratio is 1.04.Catalyst system therefor is formed (weight %): iron 90.8, aluminium 3.5, manganese 1.9, copper 2.3 and potassium 1.5.The catalyzer initial particle size is the 44-77 micron, and specific surface area is 61m2/g, and catalyst concn is 15 (weight) % in the reaction medium.
The slurries that mix of this catalyzer and whiteruss in activation pot with the hydrogen stream of 1.0NL/g-cat/h at 310 ℃ of following pre-treatment 12-48 hours.
3. pre-treatment/catalyst activated slurries are delivered to reactor continuously under nitrogen protection, with the operation loss of make-up catalyst and keep the equilibrium activity of catalyst reactor.The operational condition of synthesis reactor is: reaction pressure 2.5MPa, 270 ℃ of temperature of reaction, synthetic gas space velocity 2.0NL/g-cat/h.Per pass conversion (mole %) is: CO:76.8%, H
2: 50.8%.
4-6. with the step 4-6 among the embodiment 2.
7. under steady operation conditions, obtain following product (kg/kg-catalyzer/hour): C1-C2 0.025, and C3-C4 0.034, C
5+0.211; The latter can get (weight %) through fractionation: petroleum naphtha 56%, fraction of diesel oil 27% and wax 17%.
Embodiment 6
1. to be combined to the H2/CO mol ratio of the material synthesis gas of reaction unit be 1.0 to She Ji slurry attitude.Catalyst system therefor is formed (weight %): iron 90.8, aluminium 2.4, manganese 2.5, copper 2.8 and potassium 1.5.The catalyzer initial particle size is the 44-77 micron, and specific surface area is 61m2/g.
2-3. with step 2 and 3 among the embodiment 5, per pass conversion (mole %) is: CO:88.4%, H
2: 59.4%.
4-6. with the step 4-6 among the embodiment 2.
7. under steady operation conditions, can obtain following product (kg/kg-catalyzer/hour): C1-C2 0.048, and C3-C4 0.053, C
5+0.207; The latter can get (weight %) through fractionation: petroleum naphtha 51%, fraction of diesel oil 35% and wax 14%.
Embodiment 7
1. synthesis reaction system and the material synthesis gas identical with embodiment 1 step 1.Catalyzer is formed (weight %): iron 84.8, aluminium 5.4, manganese 2.7, copper 6.1 and potassium 1.0.The catalyzer initial particle size is the 44-77 micron, and specific surface area is 61m2/g.
2. with embodiment 1 step 2.
3. with the step 3 of embodiment 2, per pass conversion (mole %) is: CO:84.1%, H
2: 58.3%.
4-6. with the step 4-6 among the embodiment 2.
7. under steady operation conditions, can obtain following product (kg/kg-catalyzer/hour): C1-C2 0.05, and C3-C4 0.06, C
5+0.21; The latter can get (weight %) through fractionation: petroleum naphtha 53%, fraction of diesel oil 33% and wax 14%.
Embodiment 8
1. with the identical synthesis system of embodiment 1 step 1, catalyst system therefor is formed (weight %) and is: iron 82.5, aluminium 4.3, manganese 6.2, copper 2.1 and potassium 4.9.
2. with the step 2 of embodiment 1.
3-7. with embodiment 2 step 3-7, per pass conversion (mole %) is: CO:70.5%, H
2: 49.6%.Under steady operation conditions, can obtain following product (kg/kg-catalyzer/hour): C1-C2 0.03, C3-C40.03, C
5+0.19; The latter can get (weight %) through fractionation: petroleum naphtha 48%, fraction of diesel oil 38% and wax 14%.
Embodiment 9
1. with the identical synthesis system of embodiment 1 step 1, catalyst system therefor is formed (weight %) and is: iron 83.2, aluminium 5.6, manganese 8.2, copper 1.9 and potassium 1.1.
2. with the step 2 of embodiment 1.
3-7. with embodiment 2 step 3-7, per pass conversion (mole %) is: CO:73.0%, H
2: 47.1%.Under steady operation conditions, obtain following product (kg/kg-catalyzer/hour): C1-C 20.04, and C3-C4 0.06, C
5+0.22; The latter can get (weight %) through fractionation: petroleum naphtha 55%, fraction of diesel oil 34% and wax 11%.
Claims (21)
1. one kind is converted into the continuous catalysis process of hydrocarbon product with synthetic gas, and this process comprises the following steps:
The flow of feed gas that contains synthetic gas in reactor under the respective reaction condition contacts with skeletal iron catalyst particle in the slurry attitude bed, makes synthetic gas be converted into C
1-C
4Light hydrocarbon, C
5 +Product such as liquid hydrocarbon and wax,
Except the wax product, other product and by product are flowed out with vapour phase by reactor head, and are separated into gaseous by-products, light hydrocarbons gaseous product and C
5 +Liquefied hydrocarbon, the latter collects as primary product;
Draw the skeletal iron catalyst particulate slurry fluids that contains suspension by the overflow port of reactor and enter the catalyst sedimentation jar, the latter will be under the isolating condition that is suitable for granules of catalyst and wax, wherein said granules of catalyst can be deposited on described jar bottom after sedimentation, form the concentrated slurry of granules of catalyst and liquid wax;
Discharge the liquid wax that does not contain catalyzer substantially from described slurry tank top, bottom slurry tank, draw the slurries of enrichment granules of catalyst, pump into the circulation of reactor bottom as skeletal iron catalyst.
2. continuous catalysis process as claimed in claim 1 is characterized in that described process comprises following step:
The a part of fluid of discharging adds the live catalyst of a great deal of as the catalyst stream of inactivation and in reactor from catalyst recycle stream.
3. continuous catalysis process as claimed in claim 1 is characterized in that described process may further comprise the steps:
The slurries that contain catalyzer by reactor is drawn before entering the catalyst sedimentation jar, adopt waterpower to handle at cyclonic separator, to improve solid-liquid separation effect.
4. continuous catalysis process as claimed in claim 1, the reaction bed that it is characterized in that described reactor are to constitute by comprising skeletal iron catalyst particulate slurries.
5. reactor as claimed in claim 4, its characteristic manipulation condition is: temperature is 230-280 ℃ of scope, and pressure is in the 1.7-5.5MPa scope, and air speed is in the 1.0-5.0NL/g-cat/h scope.
6. continuous catalysis process as claimed in claim 1 is characterized in that also comprising in the described reactor inner tubular cooler.
7. reactor as claimed in claim 6, the liquid level that it is characterized in that slurry attitude bed wherein is controlled at by overflow port and is higher than the water cooler top.
8. continuous catalysis process as claimed in claim 1 is characterized in that described process may further comprise the steps:
The wax product of discharging through catalyst sedimentation jar top is squeezed into the catalyzer that filtration unit is removed the trace inactivation by pump, and then collects wax product;
The gained wax product is introduced flash distillation plant; Collect clean wax product from this flash tank bottom.
9. continuous catalysis process as claimed in claim 1 contains the granules of catalyst that is lower than 0.2 weight % in the liquid wax product that it is characterized in that being drawn by catalyst sedimentation jar top.
10. continuous catalysis process as claimed in claim 1 is characterized in that the catalyst concentration slurries of being drawn by described catalyst sedimentation pot bottom, throws the position that is lower than cooling tube into reactor bottom into pump, and is recycled to reactor.
11. continuous catalysis process as claimed in claim 1 is characterized in that described skeletal iron catalyst is activated or pretreated catalyzer.
12. continuous catalysis process as claimed in claim 11 is characterized in that by hydrogen or/and the heating under the nitrogen atmosphere comes the described catalyzer of activation or preconditioning.
13. continuous catalyst process as claimed in claim 1 is characterized in that the activation or preconditioning of described catalyzer ties up in the fixed-bed reactor, at hydrogen or/and carry out under the nitrogen gas stream.
14. continuous catalysis process as claimed in claim 13, the operational condition that it is characterized in that described activation or preconditioning fixed-bed reactor comprises: temperature is 300-360 ℃ of scope, pressure is in 0.1-1.0MPa gauge pressure scope, the air speed of hydrogen or nitrogen is in the 0.3-1.0NL/g-cat/h scope, and the time was 2-24 hour scope.
15. continuous catalysis process as claimed in claim 12 is characterized in that the slurries form that the activation or preconditioning of described catalyzer can catalyst/wax, feeds hydrogen or nitrogen is implemented in the catalyst activation jar.
16. continuous catalysis process as claimed in claim 15, the operational condition that it is characterized in that described catalyst activation jar is: pressure 0.1-1.0 gauge pressure scope, temperature is 250-320 ℃ of scope, and the air speed of hydrogen or nitrogen is in the 0.1-1.0NL/g-cat/h scope, and the time was 2-24 hour scope.
17. continuous catalysis process as claimed in claim 1 is characterized in that the operational condition of described catalyst sedimentation jar comprises: temperature is 230-270 ℃ of scope, and pressure is in the 1.5-5.0MPa scope, and the residence time was 15-60 minute scope.
18. continuous catalysis process as claimed in claim 1, the granules of catalyst that it is characterized in that being come out to enter by described reactor overflow the catalyst sedimentation jar has 90-99 weight % to be deposited in the bottom of described catalyst sedimentation jar.
19. continuous catalysis process as claimed in claim 1 is characterized in that it is one-pass single-pass operation that described synthetic gas transforms.
20. continuous catalysis process as claimed in claim 1 is characterized in that it is the circulation pattern operation that described synthetic gas transforms, wherein with unconverted CO and H
2Be recycled in the synthetic gas conversion reactor.
21. continuous catalysis process as claimed in claim 1, it is characterized in that entering the slurries streamline of catalyst sedimentation jar from described synthesis reactor overflow, come out to the wax liquid fluid line of strainer by catalyst sedimentation jar top, and do not establish valve control by the catalyst concentration slurries streamline that catalyst sedimentation pot bottom circulation enters synthesis reactor, all these streamlines all adopt the venturi flow table to regulate the pumpage of the described streamline of control.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US10/267,236 US6903141B2 (en) | 1999-09-21 | 2002-10-08 | Slurry-phase skeletal iron catalyst process for synthesis gas conversion to hydrocarbons |
| US10/267,236 | 2002-10-08 |
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| Publication Number | Publication Date |
|---|---|
| CN1497039A true CN1497039A (en) | 2004-05-19 |
| CN1293027C CN1293027C (en) | 2007-01-03 |
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ID=34256566
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| CNB2003101015275A Expired - Fee Related CN1293027C (en) | 2002-10-08 | 2003-10-08 | Process for preparing hydrocarbon product by synthetic gas using skeleton catalyst paste phase technology |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102264447A (en) * | 2008-12-23 | 2011-11-30 | 埃克森美孚研究工程公司 | Product filtration system for slurry reactors |
| CN103551207A (en) * | 2013-11-01 | 2014-02-05 | 神华集团有限责任公司 | Fixed fluidized bed or gas-solid bubbling bed Fischer-Tropsch catalyst reduction activation system and technique |
| CN103769241A (en) * | 2014-02-18 | 2014-05-07 | 神华集团有限责任公司 | Fixed-bed Fischer-tropsch catalyst reduction activation system and technology |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2011024650A1 (en) * | 2009-08-31 | 2011-03-03 | 独立行政法人石油天然ガス・金属鉱物資源機構 | Hydrocarbon synthesis reaction apparatus, hydrocarbon synthesis reaction system, and method for collection of liquid hydrocarbon |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2536488C2 (en) * | 1975-08-16 | 1977-08-25 | Ruhrchemie Ag | PROCESS FOR THE PRODUCTION OF UNSATATULATED HYDROCARBONS |
| US4754092A (en) * | 1985-12-30 | 1988-06-28 | Exxon Research And Engineering Company | Reducing methane production and increasing liquid yields in Fischer-Tropsch reactions |
| GB2204055B (en) * | 1987-04-29 | 1992-01-02 | Shell Int Research | Process for the preparation of hydrocarbons |
| CN1040397C (en) * | 1992-09-03 | 1998-10-28 | 中国科学院大连化学物理研究所 | Iron manganese catalyst for preparation of low carbon olefines by synthetic gas and synthetic reaction |
| US6277895B1 (en) * | 1999-09-21 | 2001-08-21 | Hydrocarbon Technologies, Inc. | Skeletal iron catalyst having improved attrition resistance and product selectivity in slurry-phase synthesis processes |
-
2003
- 2003-10-08 CN CNB2003101015275A patent/CN1293027C/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102264447A (en) * | 2008-12-23 | 2011-11-30 | 埃克森美孚研究工程公司 | Product filtration system for slurry reactors |
| CN102264447B (en) * | 2008-12-23 | 2015-02-18 | 埃克森美孚研究工程公司 | Product filtration system for slurry reactors |
| CN103551207A (en) * | 2013-11-01 | 2014-02-05 | 神华集团有限责任公司 | Fixed fluidized bed or gas-solid bubbling bed Fischer-Tropsch catalyst reduction activation system and technique |
| CN103551207B (en) * | 2013-11-01 | 2015-11-18 | 神华集团有限责任公司 | A kind of fixed fluidized bed or gas-solid bubbling bed fischer-tropsch catalysts reduction activation system and technique |
| CN103769241A (en) * | 2014-02-18 | 2014-05-07 | 神华集团有限责任公司 | Fixed-bed Fischer-tropsch catalyst reduction activation system and technology |
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| CN1293027C (en) | 2007-01-03 |
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