CN1137058A - Process for synthesizing gasoline from synthesized gas through olefin - Google Patents
Process for synthesizing gasoline from synthesized gas through olefin Download PDFInfo
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- CN1137058A CN1137058A CN 95106156 CN95106156A CN1137058A CN 1137058 A CN1137058 A CN 1137058A CN 95106156 CN95106156 CN 95106156 CN 95106156 A CN95106156 A CN 95106156A CN 1137058 A CN1137058 A CN 1137058A
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Abstract
A process for synthesizing gasoline from synthetic gas via olefin uses coal-base synthetic gas CO+H2 as raw material to synthesize gasoline through two stages. For two stage combined single cycle of tail gas, ultra-fine F-Mn catalyst particles to make CO+H2 directionally grow low-carbon olefin in the first stage and a shape selecting ZMS-5 molecular sieve catalyst is used in the second stage. An isobaric or low-pressure operation is realized. The gasoline has 142/gN cu.m(CO+H2) of yield rate and more than 90 of octane number. The percent conversion of CO is up to more than 95%. The content of 1,2,4,5-tetramethylbenzene in gasoline is less than 2%. The service life of ZMS-5 is elongated.
Description
The invention belongs to a kind of method by synthesis gas preparation gasoline, specifically it is with CO in the synthetic gas and H
2Generate low-carbon alkene and then synthesize the method for gasoline.
The seventies, the MoBil company of the U.S. successfully developed the ZMS-5 molecular sieve catalyst, then developed with the synthetic gas of Sweet natural gas base is MTG method (Tabak S, the Aand Yurchak s of raw material synthetic gasoline, Catalysis Taday, 1990,6 (3): 309), this method divides two sections to carry out, and first section is with CO and H
2Synthesize methyl alcohol, second section is that methyl alcohol synthesizes gasoline by catalyzer ZMS-5 molecular sieve, then, through simply separating, can obtain liquefied gas, gasoline and water.From report, this method all is to adopt H
2/ CO than the synthetic gas of high Sweet natural gas base as raw material.Because the per pass conversion in above-mentioned two steps are all lower, thereby have to set up two independent round-robin systems, so that improve the transformation efficiency of CO.But the investment of this recycle system is big, the process cost height, thus improved the cost of gasoline.
Afterwards, the Topsoe company of Denmark improves MTG, TIGAS method TOPP-Jorgenner J. has been proposed, Topsoe, Integrated Garoting Synthesrs, 1986), this method also is to be divided into two sections, first section synthesizes methyl alcohol and dme with synthetic gas, and second section synthesizes gasoline, the two-section joint single loop.First section is adopted composite catalyst, is raw material with Sweet natural gas base synthetic gas, and temperature of reaction 220-300 ℃, pressure 4.6MPa, second section is adopted the ZMS-5 sieve peg-raking catalyst, with methyl alcohol and dme synthetic gasoline, two-section joint single loop.Because methyl alcohol and dme synthetic is subjected to thermodynamic (al) restriction, need under elevated pressures, carry out, and the more favourable working pressure of second stage reactor is 1.5-2.5MPa, higher working pressure will produce more durol and water vapor, can make two sections ZMS-5 molecular sieve that irreversible poisoning takes place.This brings certain difficulty just for the pressure operation of two reactor in the best condition.
The objective of the invention is to develop a kind of yield of gasoline height, quality better, hydrocarbon yield height, one or two sections methods that working pressure matches by the synthesized gas through olefin synthetic gasoline.
The present invention is raw material with the coal based synthetic gas, synthesizes gasoline through two sections, the two-section joint single loop, and second section is adopted the ZMS-5 molecular sieve catalyst, it is characterized in that first section has been adopted and can make CO+H
2The directed Fe-Mn Ultra-fine Particle Catalysts that generates low-carbon alkene.
The Fe/Mn weight ratio of described catalyzer is (3～2): 1, and granularity is less than 10nm, and specific surface is 100m
2/ g～200m
2/ g, pore volume are 0.2ml/g～0.5ml/g.This Preparation of catalysts method was divided into for two steps, and the first step obtains the oxyhydroxide of Fe/Mn oxalate mixture or Fe/Mn by chemosynthesis; Second step obtained the catalyzer of ultrafine particle by the control degradation method.The method for making of described Fe/Mn oxalate mixture is: iron powder and manganese acetate are added in the aqueous acetic acid; under nitrogen protection, be heated backflow; after iron powder dissolves fully; add rapidly oxalic acid aqueous solution and precipitate, throw out after filtration, promptly get Fe/Mn oxalate mixture after the washing, drying.The method for making of described Fe/Mn oxyhydroxide is: adopt conventional coprecipitation method, iron nitrate and manganous nitrate are dissolved in the water, precipitate with ammoniacal liquor, throw out after filtration, promptly get Fe/Mn oxyhydroxide after the washing, drying.
The detailed content of this invention and effect reach embodiment in conjunction with the accompanying drawings and are described as follows:
Fig. 1 is the laboratory reaction apparatus schema.
As shown in the figure: 1 is mixing tank, and 2 for giving hot device, and 3 is first stage reactor, interior dress Fe/Mn ultrafine particle.Catalyzer 100ml, 4 is second stage reactor, interior dress ZMS-5 molecular sieve 100ml, 5 is condenser, and 6 is separator, and 7 is the pump anterior bumper, and 8 is the pump posterior bumper, and 9 is recycle pump, and 10 is wet flow indicator, and F is a raw material, G is discharging gas.
As shown in Figure 1, delay through the coal-based synthetic raw gas after desulfurization, deoxidation, the pressurization and after coming self-pumping Rush the tail gas of device 8 in blender 1 interior mixing, give heat after hot device 2 and to one section reaction temperature, enter one Section reactor 3, this reactor are the fixed bed reaction that is provided with water-cooled or oil cooling chuck control reaction temperature Device, in-built Fe/Mn Ultra-fine Particle Catalysts 100ml, the intermediate products such as low-carbon alkene that reaction generates, Directly enter second stage reactor 4, in-built ZMS-5 molecular sieve catalyst 100ml, at this with intermediate product Orientation synthesizes gasoline etc., and product carries out gas-liquid separation, liquid through condenser 5 condensations in separator 6 Attitude product gasoline etc. is emitted from the bottom, the emptying after wet flow indicator 13 meterings of tail gas small part, big section Divide tail gas after pump anterior bumper 9 enters circulating pump 9 pressurizations, to recycle.
Embodiment 1
Adopt flow process as described in Figure 1, the basic technology parameter of this test is: 335 ℃ of one section temperature of reaction, and 325 ℃ of second-stage reaction temperature, system pressure is 2.5MPa (pressure does not have obvious influence), during air speed 500/, unstripped gas H
2/ CO ratio is 2, and recycle ratio is 3.One section reacted products distribution is as follows: C
1 013.57%, C
2 82.58%, C
2 07.17%, C
3 61.64%, C
3 =9.76%, C
4 01.14%, C
4 =5.85%, C
5-C
1958.29%, wherein alkene accounts for more than 50%, C
2 =～C
4 =/ C
2-C
4=80.95%.Its test-results is: the CO transformation efficiency is 96%, (below be all W%), and hydrocarbon-selective is 93%, CO
2Selectivity is 7%, and the vapour yield is 143g/Nm
3(CO+H
2), when the gasoline space-time yield is the 0.098ml/ml catalyzer.Behind the second-stage reaction, the consisting of of gasoline: with C benchmark, C
5-C
11Be 98.2%, C
12-C
15Be 1.8%, the consisting of of hydro carbons in the gasoline: aromatic hydrocarbons 27.5% durol＜2%, alkene 13.7%, isoparaffin 30.1%, normal paraffin 12.5%, cyclic hydrocarbon hydrocarbon 8.8%, unknown material 7.3%, gasoline rate alkane value 91.5.
Embodiment 2
Flow process and condition are basic identical with embodiment 1, and difference is that one section temperature of reaction is 328 ℃, and air speed is 1000/ o'clock, and one section reacted products distribution is as follows: C
1 014.36%, C
2 02.58%, C
2 =7.47%, C
3 01.79%, C
3 =9.81%, C
4 01.40%, C
4 =7.32%, C
5 +55.27%, C wherein
2 =～C
4 =/ C
2～C
4=81.00%.Its result is a CO transformation efficiency 94.1%, hydrocarbon-selective 90.8%, yield of gasoline 123.8g/Nm
3(CO+H
2), when the gasoline space-time yield is the 0.17ml/ml catalyzer.
With at present in the world state-of-the-art TIGAS method compare, technological progress of the present invention be aobvious and Easily see. Please see following table.
(videing infra)
| The present invention | The TIGAS method | |
| Unstripped gas | Coal-based | The natural gas base |
| Catalyst system | Fe/Mn---ZMS-5 | Composite catalyst--ZMS-5 |
| Reaction temperature ℃ 1 section 2 sections | 270-330 270-360 | 220-300 350-400 |
| 1 section 2 sections of reaction pressure MPa | 2.5 2.5 | 4.6 5.4 |
| Unstripped gas H2/CO | 1.9-2.1 | 2.0 |
| The circulation of tail gas ratio | 3 | 5 |
| CO conversion ratio % | 95.8 | 98.0 |
| Hydrocarbon-selective % | 94.2 | 74.1 |
| Product distribution % CH4 C 2 C 3-C 4 C 5-C 11 | 15.3 3.1 7.1 74.5 | 4.8 3.8 16.3 75.1 |
| Hydrocarbon yield g/Nm3(CO+H 2) | 197.0 | 151.2 |
| Yield of gasoline g/NM3(CO+H 2) | 142 | 113.4 |
Contrast shows that the present invention has the following advantages:
1. one, two section pressure matches, and has realized desirable press operation such as grade, its operating pressure Only have 1/2 of TIGAS, thereby greatly reduce cost and the running expense of equipment.
2. yield of gasoline of the present invention is up to 142/gNm
3(CO+H
2) more than, this is in the world with incomparable in the class methods.
3. under lower tail gas recycle ratio, realized the high conversion (＞95%) of CO, realized the highly selective (＞94%) of the high yield and the hydro carbons of hydro carbons simultaneously, this shows that the present invention is good to the directional property of purpose product.
4. the mensuration of gasoline composition and quality shows, gasoline soldier alkane value is more than 90.
5. because two sections operations under low pressure, the growing amount of durol is below 2%, thereby prolonged the regeneration period of ZMS-5 greatly, behind its active decline, only by burning its activity recovered fully, almost do not have irreversible poisoning.
Claims (5)
1. the method by the synthesized gas through olefin synthetic gasoline is a raw material with the synthetic gas, synthesizes gasoline through two sections, and tail gas two-section joint single loop takes ZMS-5 shape to select molecular sieve catalyst for second section, it is characterized in that first section has been adopted and can make CO+H
2The directed Fe-Mn Ultra-fine Particle Catalysts that generates low-carbon alkene, the Fe/Mn weight ratio of this catalyzer is (3-2): 1, granularity is less than 10nm, and specific surface is 100m
2/ g～200m
2/ g, pore volume are 0.2ml/g～0.5ml/g, and this catalyzer is that the control degradation method by the oxyhydroxide of Fe/Mn oxalate mixture or Fe/Mn makes.
2. the method for claim 1, its feature is identical one, two section reaction pressure.
3. method as claimed in claim 2, its feature is 2.5MPa one, two section reaction pressure.
4. method as claimed in claim 1 or 2 is characterized in that described raw material of synthetic gas is a coal based synthetic gas.
5. method as claimed in claim 1 or 2, the intermediate product that it is characterized in that a section is a low-carbon alkene.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN95106156A CN1054832C (en) | 1995-05-26 | 1995-05-26 | Process for synthesizing gasoline from synthesized gas through olefin |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN95106156A CN1054832C (en) | 1995-05-26 | 1995-05-26 | Process for synthesizing gasoline from synthesized gas through olefin |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1137058A true CN1137058A (en) | 1996-12-04 |
| CN1054832C CN1054832C (en) | 2000-07-26 |
Family
ID=5075769
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN95106156A Expired - Lifetime CN1054832C (en) | 1995-05-26 | 1995-05-26 | Process for synthesizing gasoline from synthesized gas through olefin |
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| Country | Link |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105473495A (en) * | 2013-07-31 | 2016-04-06 | 沙特基础工业公司 | A process for the production of olefins through fischer-tropsch based synthesis |
| US9701910B2 (en) | 2013-07-31 | 2017-07-11 | Saudi Basic Industries Corporation | Process for the production of olefins through FT based synthesis |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB8309585D0 (en) * | 1983-04-08 | 1983-05-11 | British Petroleum Co Plc | Catalyst composition |
| US4708857A (en) * | 1983-07-26 | 1987-11-24 | Centre De Recherche Industrielle Du Quebec | Process for preparing a crystalline iron-borosilicate |
| US4728672A (en) * | 1984-10-08 | 1988-03-01 | Research Association For Petroleum Alternatives Development | Process for producing hydrocarbons |
| CN1015171B (en) * | 1986-01-09 | 1991-12-25 | 英国石油公司 | Improved syngas conversion catalyst |
-
1995
- 1995-05-26 CN CN95106156A patent/CN1054832C/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105473495A (en) * | 2013-07-31 | 2016-04-06 | 沙特基础工业公司 | A process for the production of olefins through fischer-tropsch based synthesis |
| US9695365B2 (en) | 2013-07-31 | 2017-07-04 | Saudi Basic Industries Corporation | Process for the production of olefins through FT based synthesis |
| US9701910B2 (en) | 2013-07-31 | 2017-07-11 | Saudi Basic Industries Corporation | Process for the production of olefins through FT based synthesis |
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| Publication number | Publication date |
|---|---|
| CN1054832C (en) | 2000-07-26 |
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Owner name: ZHONGKE SYNTHETIC OIL TECHNOLOGY CO., LTD., DISTR Free format text: FORMER OWNER: SHANXI INST. OF COAL CHEMISTRY, CHINESE ACADEMY OF SCIENCES Effective date: 20060915 |
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Effective date of registration: 20060915 Address after: 030006 Taiyuan hi tech Zone, South Central Cyberport, port 4, zone 2, A and B Patentee after: Zhongke Synthetic Oil Technology Co., Ltd. Address before: 165 mailbox 030001, Shanxi City, Taiyuan Province Patentee before: Shanxi Institute of Coal Chemistry, Chinese Academy of Sciences |
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Address after: 101407 Beijing city Huairou District Yanqi Economic Development Zone C District No. 1 south two Street Park Patentee after: Zhongke Synthetic Oil Technology Co., Ltd. Address before: 030006, Taiyuan hi tech Zone, Shanxi, South Central Cyberport, port 4, 2, A and B Patentee before: Zhongke Synthetic Oil Technology Co., Ltd. |
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Expiration termination date: 20150526 Granted publication date: 20000726 |