US3506590A - Manufacture of synthesis-,hydrogenating-,or reduction-gas - Google Patents
Manufacture of synthesis-,hydrogenating-,or reduction-gas Download PDFInfo
- Publication number
- US3506590A US3506590A US711919A US3506590DA US3506590A US 3506590 A US3506590 A US 3506590A US 711919 A US711919 A US 711919A US 3506590D A US3506590D A US 3506590DA US 3506590 A US3506590 A US 3506590A
- Authority
- US
- United States
- Prior art keywords
- gas
- coking
- hydrogenating
- synthesis
- coke
- 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 - Lifetime
Links
- 238000004519 manufacturing process Methods 0.000 title description 10
- 239000007789 gas Substances 0.000 description 44
- 238000004939 coking Methods 0.000 description 24
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 12
- 238000000034 method Methods 0.000 description 11
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 9
- 229910052799 carbon Inorganic materials 0.000 description 9
- 229930195733 hydrocarbon Natural products 0.000 description 9
- 150000002430 hydrocarbons Chemical class 0.000 description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 8
- 239000003245 coal Substances 0.000 description 7
- 239000000571 coke Substances 0.000 description 7
- 239000000463 material Substances 0.000 description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- 239000001257 hydrogen Substances 0.000 description 6
- 229910052739 hydrogen Inorganic materials 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 239000003575 carbonaceous material Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
Definitions
- coke-oven gas and also the carbon-rich materials produced in the usual coking process are replaced by oil gas and natural gas charges of the ever-growing displacement process and a profitability-favourable charge of coke-oven gas for the production of the abovenoted products is no longer presented.
- the invention is accordingly directed to the problem of creating a process for obtaining synthesis-,.hydrogenating-, or reduction-gas, in which readily available coal is used as starting material and in which neither carbon in diflicultly us'able form nor the increasingly more difiicult- 1y disposable or workable coke-oven gas is produced.
- a process for the manufacture of synthesis-, hydrogenating, or reduction-gas characterised in that coal is coked in a chamher at such high temperature and/or coking speed that the crude gas has the desired composition for further treatment to synthesis-, hydrogenating, or reduction-gas by purification and has a low content of carbon-rich material.
- the invention is based on the discovery that through an increase of the coking temperature and/or coking speed lying fully within the framework of technical possibilities, the carbon-rich materials contained in the coke-oven gas are already cracked in the chamber to a much predominating proportion, so that the carbon produced from the carbon-rich materials remains in the chamber together with the coke and can be used with this.
- the proportion of the hydrocarbons or carbon-rich materials respectively remaining in the coke-oven gas can by the selection of the coking temperature and/ or the coking speed be limited to that amount in which an economical treatment of the crude gas to the synthesis-, hydrogenating-, or reductiongas, by purification is possible.
- the coking temperature and/or the coking speed are preferably more than 1450 C. and 15 mm/h. respectively.
- the further treatment of the crude gas to synthesis-, hydrogenating-, 0r reduction-gas can be effected by cooling the crude gas in known manner, whereby a rich gas fraction containing hydrocarbons still present in it is separated from the crude gas.
- This rich gas fraction contains as impurity hydrogen sulphide in relatively high concentration, so that the separation of this impurity from the rich gas fraction in a known manner can be carried out under economically very favourable conditions.
- the purified rich gas fraction can then be used for heating the chamber or for chemical purposes.
- a coking speed of about 12 mm./h. a coke oven gas is obtained which contains about 55% hydrogen, 27% methane, 5 to 6% carbon monoxide, and about 5% nitrogen as well as carbon dioxide and heavy hydrocarbons, namely between 2.5 to 4.5% tar, 0.6 to 1.5% benzene as well as 0.2 to 0.3% ammonia and 0.3 to 0.7% hydrogen sulphide, there results in the process according to the invention with a coking temperature of about 1550 C., a coking time of about 10 hours and a coking speed of about 22 mm./h., a crude gas which contains about 70 to hydrogen, 7 to 15% of carbon monoxide, small amounts of nitrogen, carbon dioxide and methane as well as about 0.2% tar, 0.1% benzene, 0 to 0.2% ammonia and about 0.5 to 1% of hydrogen sulphide.
- the further treatment of the crude gas takes place in known manner, for example by supercooling.
- hydrogenating hydrogen or a synthesis gas fraction is obtained, which contains essentially hydrogen and carbon monoxide as well as nitrogen and is free from hydrocarbons.
- the separated rich gas fraction contains essentially methane, carbon dioxide, heavy hydrocarbons and hydrogen sulphide.
- the hydrogen sulphide portion of the crude gas obtained in the process according to the invention is higher than in conventional coke-oven gas, its removal according to known processes from the rich gas fraction presents no difficulties, since the hydrogen sulphide is present there in relatively high concentration.
- the high hydrogen sulphide content of the crude gas is attributable to an extensive desulphurisation of the coke, which favours its use for metallurgical purposes.
- the coke is obtained in relatively small pieces and in this form is particularly well adapted for use in a blast furnace. It is furthermore noteworthy that the ammonia is produced, if at all, only in very small amounts, which is particularly advantageous since this product only rarely can be obtained and utilised under economically tolerable conditions.
- Process for the production of a gas having a relatively high content of hydrogen and a relatively low content of hydrocarbon which comprises coking coal in a chamber, Without the admission of gases into the chamber, at a coking temperature between about 1450" C. and about 1550 C., and a coking speed between about 15 and about 22 mm./hour to provide a crude gas having a low content of carbon rich material and then purifying said crude gas by removing at least hydrocarbons, carbon dioxide and hydrogen sulfide.
- Process for the production of a gas having a relatively high content'of hydrogen and a relatively low content of hydrocarbon which comprises coking coal in a chamber, without the admission of gases into the chamber, at a coking temperature of at least about 1450" C. and a coking speed of at least about 15 mm./hour, to provide 5 a crude gas having a low content of carbon rich material.
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Materials Engineering (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Industrial Gases (AREA)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEH0062106 | 1967-03-11 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US3506590A true US3506590A (en) | 1970-04-14 |
Family
ID=7161724
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US711919A Expired - Lifetime US3506590A (en) | 1967-03-11 | 1968-03-11 | Manufacture of synthesis-,hydrogenating-,or reduction-gas |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US3506590A (en)van) |
| BE (1) | BE711854A (en)van) |
| DE (1) | DE1667542B2 (en)van) |
| FR (1) | FR1561525A (en)van) |
| GB (1) | GB1204257A (en)van) |
| NL (1) | NL6802091A (en)van) |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB191319872A (en) * | 1912-09-02 | Ofenbau Gmbh | Process of, and Apparatus for, the Dry Distillation of Coal and the like. | |
| US989324A (en) * | 1909-09-27 | 1911-04-11 | Christian Bolz | Art of producing gases in upright retorts. |
| GB100952A (en)van) * | 1915-07-17 | 1916-09-07 | Gerardus Aarts Jacobus | |
| US2209255A (en) * | 1938-12-05 | 1940-07-23 | Shawinigan Chem Ltd | Coke production |
| US2691573A (en) * | 1950-12-15 | 1954-10-12 | Phillips Petroleum Co | Desulfurization in the gasification of coal |
| US2885327A (en) * | 1956-05-14 | 1959-05-05 | Consolidation Coal Co | Process of coking solid carbonizable material |
| US2982701A (en) * | 1958-09-30 | 1961-05-02 | California Research Corp | Retorting and coking of bituminous solids |
-
1967
- 1967-03-11 DE DE1667542A patent/DE1667542B2/de active Granted
-
1968
- 1968-02-14 NL NL6802091A patent/NL6802091A/xx unknown
- 1968-03-06 GB GB00788/68A patent/GB1204257A/en not_active Expired
- 1968-03-07 FR FR1561525D patent/FR1561525A/fr not_active Expired
- 1968-03-08 BE BE711854D patent/BE711854A/xx unknown
- 1968-03-11 US US711919A patent/US3506590A/en not_active Expired - Lifetime
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US989324A (en) * | 1909-09-27 | 1911-04-11 | Christian Bolz | Art of producing gases in upright retorts. |
| GB191319872A (en) * | 1912-09-02 | Ofenbau Gmbh | Process of, and Apparatus for, the Dry Distillation of Coal and the like. | |
| GB100952A (en)van) * | 1915-07-17 | 1916-09-07 | Gerardus Aarts Jacobus | |
| US2209255A (en) * | 1938-12-05 | 1940-07-23 | Shawinigan Chem Ltd | Coke production |
| US2691573A (en) * | 1950-12-15 | 1954-10-12 | Phillips Petroleum Co | Desulfurization in the gasification of coal |
| US2885327A (en) * | 1956-05-14 | 1959-05-05 | Consolidation Coal Co | Process of coking solid carbonizable material |
| US2982701A (en) * | 1958-09-30 | 1961-05-02 | California Research Corp | Retorting and coking of bituminous solids |
Also Published As
| Publication number | Publication date |
|---|---|
| GB1204257A (en) | 1970-09-03 |
| DE1667542C3 (en)van) | 1975-05-07 |
| FR1561525A (en)van) | 1969-03-28 |
| DE1667542A1 (de) | 1971-09-23 |
| BE711854A (en)van) | 1968-07-15 |
| DE1667542B2 (de) | 1974-08-22 |
| NL6802091A (en)van) | 1968-09-12 |
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