CN108192649A - The process system and its control method of hydrogen are directly produced based on coke oven - Google Patents
The process system and its control method of hydrogen are directly produced based on coke oven Download PDFInfo
- Publication number
- CN108192649A CN108192649A CN201810104747.XA CN201810104747A CN108192649A CN 108192649 A CN108192649 A CN 108192649A CN 201810104747 A CN201810104747 A CN 201810104747A CN 108192649 A CN108192649 A CN 108192649A
- Authority
- CN
- China
- Prior art keywords
- hydrogen
- coal
- vertical tube
- branch
- gas
- 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.)
- Granted
Links
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 67
- 239000001257 hydrogen Substances 0.000 title claims abstract description 65
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 65
- 238000000034 method Methods 0.000 title claims abstract description 38
- 239000000571 coke Substances 0.000 title claims abstract description 37
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 39
- 239000007789 gas Substances 0.000 claims abstract description 36
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000003245 coal Substances 0.000 claims abstract description 31
- 238000003763 carbonization Methods 0.000 claims abstract description 27
- 239000003034 coal gas Substances 0.000 claims abstract description 26
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 20
- 238000005406 washing Methods 0.000 claims abstract description 20
- 238000004064 recycling Methods 0.000 claims abstract description 17
- 238000000746 purification Methods 0.000 claims abstract description 16
- 239000007921 spray Substances 0.000 claims abstract description 9
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 7
- 238000000197 pyrolysis Methods 0.000 claims description 10
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 9
- 239000000908 ammonium hydroxide Substances 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 8
- 238000006477 desulfuration reaction Methods 0.000 claims description 6
- 230000023556 desulfurization Effects 0.000 claims description 6
- 238000010025 steaming Methods 0.000 claims description 5
- 239000011269 tar Substances 0.000 description 15
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 3
- 229910000831 Steel Inorganic materials 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 239000012717 electrostatic precipitator Substances 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000000137 annealing Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000009615 deamination Effects 0.000 description 1
- 238000006481 deamination reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000005096 rolling process Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 229930195735 unsaturated hydrocarbon Natural products 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
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/18—Modifying the properties of the distillation gases in the oven
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/52—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
- C10K1/028—Dust removal by electrostatic precipitation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
- C10K1/046—Reducing the tar content
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Dispersion Chemistry (AREA)
- Industrial Gases (AREA)
Abstract
The invention discloses a kind of process system that hydrogen is directly produced based on coke oven, including：Vertical tube, triple valve and the coal-gas recovering purification branch being connect with triple valve and hydrogen recycling branch, vertical tube are located at the top of carbonization chamber, are equipped with ammonia spray device on vertical tube, the exit of vertical tube is equipped with triple valve；Coal-gas recovering purification branch includes sequentially connected first gas collecting tube, primary cooler, the first electric tar, desulfurizing tower, the first Ammonic washing tower and washes benzene column；Hydrogen recycling branch includes being sequentially connected the second gas collecting tube, the second Ammonic washing tower and the second electric tar；When the temperature of carbonization chamber center coal is less than or equal to preset temperature, control triple valve makes vertical tube be connected with coal-gas recovering purification branch；When the temperature of carbonization chamber center coal is more than preset temperature, control triple valve makes vertical tube be connected with hydrogen recycling branch.The process system proposed by the present invention that hydrogen is directly produced based on coke oven reduces recycling hydrogen gas in coke oven gas cost.
Description
Technical field
The present invention relates to coke-stove gas processing technology field more particularly to a kind of techniques that hydrogen is directly produced based on coke oven
System and its control method.
Background technology
Coke oven be coal is heated under conditions of air is completely cut off destructive distillation generate coke stove, coal in retort process simultaneously
Coke-stove gas is generated, the main component of coke-stove gas is H2（55%~60%）And CH4（23%~27%）, in addition also contain a small amount of CO
（5%~8%）、C2More than unsaturated hydrocarbons（2%~4%）、CO2（1.5%~3%)、O2 (0.3%~0.8%))、N2(3% ~ 7%) etc., coke-oven coal
Gas belongs to middle calorific value of gas, and calorific value is 17 ~ 19MJ/Nm3, it is a kind of important secondary energy sources.The hydrogeneous tolerance of oven gas is high, leads to
The hydrogen of high-purity can be generated by crossing pressure-variable adsorption, and hydrogen is a kind of new energy fuel of cleaning, can also be used as the original of synthesis ammonia
Material, protection gas of the steel station-service hydrogen as steel rolling bright annealing.
Containing plurality of impurities such as tar, benzene, naphthalene, sulfide, ammonia, hydride hydrogens in the raw coke oven gas that coke oven initially generates, need
Clean coke-stove gas can be just obtained by multiple processes such as first cold, desulfurization, deamination, de- benzene, clean coke-stove gas is as change
The raw material of pressure absorption hydrogen making.But generating the hydrogen of high-purity again by clean coke-stove gas at present, cost is higher.
Invention content
The process system and its controlling party of hydrogen are directly produced it is a primary object of the present invention to provide a kind of based on coke oven
Method, it is intended to reduce recycling hydrogen gas in coke oven gas cost.
To achieve the above object, the present invention provides a kind of process system that hydrogen is directly produced based on coke oven, including：It is perpendicular
Pipe, triple valve and the coal-gas recovering purification branch being connect with triple valve and hydrogen recycling branch, wherein,
The vertical tube is located at the top of carbonization chamber, is equipped with ammonia spray device on vertical tube, the exit of vertical tube is equipped with triple valve；
Coal-gas recovering purification branch includes sequentially connected first gas collecting tube, primary cooler, the first electric tar, desulfurizing tower, the
One Ammonic washing tower and wash benzene column；
The hydrogen recycling branch includes being sequentially connected the second gas collecting tube, the second Ammonic washing tower and the second electric tar；
When the temperature of carbonization chamber center coal is less than or equal to preset temperature, control triple valve makes vertical tube purify branch with coal-gas recovering
Road connects；When the temperature of carbonization chamber center coal is more than preset temperature, control triple valve makes vertical tube be connected with hydrogen recycling branch.
Preferably, it is provided with the first air blower between the first electric tar and desulfurizing tower of the coal-gas recovering purification branch.
Preferably, the second electric tar rear of the hydrogen recycling branch is provided with the second air blower.
Preferably, first Ammonic washing tower and the second Ammonic washing tower are connect with ammonia steaming device.
Preferably, the process system that hydrogen is directly produced based on coke oven further includes what is be electrically connected with the triple valve
Controller, carbonization chamber inside set the temperature measuring equipment for measuring carbonization chamber center coal temperature, controller and temperature survey
Device is electrically connected.
Present invention further propose that a kind of control method for the process system that hydrogen is directly produced based on above-mentioned coke oven, including
Following steps：
At dry distillation of coal initial stage, control triple valve makes vertical tube be connected with coal-gas recovering purification branch, and coke-stove gas is sprayed by vertical tube
Ammonium hydroxide cooling after, into coal-gas recovering purify branch in cooled down successively, tar removing, desulfurization, except ammonia and except benzene processing after, obtain
To purified gas；
After the temperature of carbonization chamber center coal is more than preset temperature, control threeway Vavle switching makes vertical tube recycle branch company with hydrogen
Logical, after coke-stove gas sprays ammonium hydroxide cooling by vertical tube, the second Ammonic washing tower that branch is recycled by hydrogen is highly concentrated except being obtained after ammonia
The hydrogen of degree.
Preferably, the preset temperature is 750 DEG C.（The set temperature is related with coal, is about for general mixed coal
750℃）.
The process system proposed by the present invention that hydrogen is directly produced based on coke oven, is had the advantages that：
1st, the hydrogen of the direct commercial coke oven coal gas of coke oven and concentration higher than 95% can be realized simultaneously, while it recycles hydrogen cost
It is low；
2nd, while electrostatic precipitator efficiency of dust collection and dedusting stability is ensured, the gas cooler of original system can be cancelled,
So as to simplify system.
Description of the drawings
Fig. 1 is the structure diagram for the process system that hydrogen is directly produced the present invention is based on coke oven.
In figure, 10- vertical tubes, 20- triple valves, the first gas collecting tubes of 31-, 32- primary coolers, the first electric tars of 33-, 34- desulfurization
Tower, the first Ammonic washing towers of 35-, 36- wash benzene column, the first air blowers of 37-, the second gas collecting tubes of 41-, the second Ammonic washing towers of 42-, 43- second
Electric tar, the second air blowers of 44-, 50- ammonia steaming devices.
The embodiments will be further described with reference to the accompanying drawings for the realization, the function and the advantages of the object of the present invention.
Specific embodiment
It should be appreciated that the specific embodiments described herein are merely illustrative of the present invention, it is not intended to limit the present invention.
The present invention proposes a kind of process system that hydrogen is directly produced based on coke oven.
In this preferred embodiment, a kind of process system that hydrogen is directly produced based on coke oven, including：Vertical tube 10, triple valve
20 and connect with triple valve 20 coal-gas recovering purification branch and hydrogen recycling branch, wherein,
Vertical tube 10 is located at the top of carbonization chamber, is equipped with ammonia spray device on vertical tube 10, the exit of vertical tube 10 is equipped with threeway
Valve 20；
Coal-gas recovering purification branch includes sequentially connected first gas collecting tube 31, primary cooler 32, the first electric tar 33, desulfurizing tower
34th, the first Ammonic washing tower 35 and benzene column 36 is washed；
Hydrogen recycling branch includes being sequentially connected the second gas collecting tube 41, the second Ammonic washing tower 42 and the second electric tar 43；
When the temperature of carbonization chamber center coal is less than or equal to preset temperature, control triple valve 20 makes vertical tube 10 and coal-gas recovering net
Change branch connection；When the temperature of carbonization chamber center coal is more than preset temperature, control triple valve 20 makes vertical tube 10 be recycled with hydrogen
Branch connects.
Further, it is provided with the first air blower between coal-gas recovering purification the first electric tar 33 of branch and desulfurizing tower 34
37.43 rear of the second electric tar of hydrogen recycling branch is provided with the second air blower 44.
First Ammonic washing tower 35 and the second Ammonic washing tower 42 are connect with ammonia steaming device 50.By ammonia steaming device 50 in Ammonic washing tower
Ammonium hydroxide recycled.
Further, the process system that hydrogen is directly produced based on coke oven further includes the control being electrically connected with triple valve 20
Device, carbonization chamber inside set the temperature measuring equipment for measuring carbonization chamber center coal temperature, controller and temperature measuring equipment
Electrical connection.
By setting controller, so as to fulfill switching is automatically controlled, reduce manual operation.Because the temperature of destructive distillation coal be from
Both sides are constantly raised toward center, and when the temperature of carbonization chamber center coal reaches 750 DEG C, triple valve just is switched to hydrogen recycling
Branch.
Coke oven has many group carbonization chambers to compose in parallel, and each carbonization chamber is mutual indepedent, and coal is in carbonization chamber during destructive distillation
Between about in 18-22h, coal mainly generates methane, hydrogen sulfide, tar, benzene and homologue, naphthalene etc. at destructive distillation initial stage, with destructive distillation temperature
The raising of degree, the content of hydrogen are continuously improved, and are hydrogen in the almost all that destructive distillation later stage coal releases in Coking Process.
Therefore, the process system that hydrogen is directly produced based on coke oven is switched in time according to the temperature of carbonization chamber center coal.
It is as follows that the process system of hydrogen its operation principle is directly produced based on coke oven.
At dry distillation of coal initial stage, control triple valve 20 makes vertical tube 10 be connected with coal-gas recovering purification branch, and coke-stove gas passes through
After vertical tube 10 sprays ammonium hydroxide cooling, purified in branch into coal-gas recovering and cooled down successively, tar removing, desulfurization, except ammonia and removed
After benzene processing, purified gas is obtained；
When the temperature of carbonization chamber center coal is more than preset temperature（750℃）Afterwards, the switching of control triple valve 20 makes vertical tube 10 and hydrogen
Branch connection is recycled, after coke-stove gas sprays ammonium hydroxide cooling by vertical tube 10, passes through the second Ammonic washing tower 42 that hydrogen recycles branch
Except the hydrogen that high concentration is obtained after ammonia.
The process system proposed by the present invention that hydrogen is directly produced based on coke oven, is had the advantages that：
1st, the hydrogen of the direct commercial coke oven coal gas of coke oven and concentration higher than 95% can be realized simultaneously, while it recycles hydrogen cost
It is low；
2nd, while electrostatic precipitator efficiency of dust collection and dedusting stability is ensured, the gas cooler of original system can be cancelled,
So as to simplify system.
Present invention further propose that a kind of control method for the process system that hydrogen is directly produced based on coke oven.
In this preferred embodiment, a kind of control method for the process system that hydrogen is directly produced based on coke oven, including following
Step：
At dry distillation of coal initial stage, control triple valve makes vertical tube be connected with coal-gas recovering purification branch, and coke-stove gas is sprayed by vertical tube
Ammonium hydroxide cooling after, into coal-gas recovering purify branch in cooled down successively, tar removing, desulfurization, except ammonia and except benzene processing after, obtain
To purified gas；
After the temperature of carbonization chamber center coal is more than preset temperature, control threeway Vavle switching makes vertical tube recycle branch company with hydrogen
Logical, after coke-stove gas sprays ammonium hydroxide cooling by vertical tube, the second Ammonic washing tower that branch is recycled by hydrogen is highly concentrated except being obtained after ammonia
The hydrogen of degree.
Specifically, preset temperature is 750 DEG C.（The set temperature is related with coal, is about 750 for general mixed coal
℃）.
It these are only the preferred embodiment of the present invention, be not intended to limit the scope of the invention, it is every to utilize this hair
The equivalent structure transformation that bright specification and accompanying drawing content are made directly or indirectly is used in other related technical areas,
Similarly it is included within the scope of the present invention.
Claims (7)
1. a kind of process system that hydrogen is directly produced based on coke oven, which is characterized in that including：Vertical tube, triple valve and with three
The coal-gas recovering purification branch of port valve connection and hydrogen recycling branch, wherein,
The vertical tube is located at the top of carbonization chamber, is equipped with ammonia spray device on vertical tube, the exit of vertical tube is equipped with triple valve；
Coal-gas recovering purification branch includes sequentially connected first gas collecting tube, primary cooler, the first electric tar, desulfurizing tower, the
One Ammonic washing tower and wash benzene column；
The hydrogen recycling branch includes being sequentially connected the second gas collecting tube, the second Ammonic washing tower and the second electric tar；
When the temperature of carbonization chamber center coal is less than or equal to preset temperature, control triple valve makes vertical tube purify branch with coal-gas recovering
Road connects；When the temperature of carbonization chamber center coal is more than preset temperature, control triple valve makes vertical tube be connected with hydrogen recycling branch.
2. the process system of hydrogen is directly produced based on coke oven as described in claim 1, which is characterized in that the coal-gas recovering
The first air blower is provided between the first electric tar and desulfurizing tower of purification branch.
3. the process system of hydrogen is directly produced based on coke oven as described in claim 1, which is characterized in that the hydrogen recycling
Second electric tar rear of branch is provided with the second air blower.
4. the process system of hydrogen is directly produced based on coke oven as described in claim 1, which is characterized in that described first washes ammonia
Tower and the second Ammonic washing tower are connect with ammonia steaming device.
5. the process system that hydrogen is directly produced based on coke oven as described in any one in Claims 1-4, feature are existed
In further including the controller being electrically connected with the triple valve, setting is for measuring carbonization chamber center coal temperature inside carbonization chamber
Temperature measuring equipment, controller are electrically connected with temperature measuring equipment.
6. a kind of control of process system that hydrogen is directly produced based on coke oven as described in any one in claim 1 to 5
Method, which is characterized in that include the following steps：
At dry distillation of coal initial stage, control triple valve makes vertical tube be connected with coal-gas recovering purification branch, and coke-stove gas is sprayed by vertical tube
Ammonium hydroxide cooling after, into coal-gas recovering purify branch in cooled down successively, tar removing, desulfurization, except ammonia and except benzene processing after, obtain
To purified gas；
After the temperature of carbonization chamber center coal is more than preset temperature, control threeway Vavle switching makes vertical tube recycle branch company with hydrogen
Logical, after coke-stove gas sprays ammonium hydroxide cooling by vertical tube, the second Ammonic washing tower that branch is recycled by hydrogen is highly concentrated except being obtained after ammonia
The hydrogen of degree.
7. the control method of the process system of hydrogen is directly produced based on coke oven as claimed in claim 6, which is characterized in that institute
It is 750 DEG C to state preset temperature.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810104747.XA CN108192649B (en) | 2018-02-02 | 2018-02-02 | Process system for directly producing hydrogen based on coke oven and control method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810104747.XA CN108192649B (en) | 2018-02-02 | 2018-02-02 | Process system for directly producing hydrogen based on coke oven and control method thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108192649A true CN108192649A (en) | 2018-06-22 |
| CN108192649B CN108192649B (en) | 2020-01-14 |
Family
ID=62591962
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810104747.XA Expired - Fee Related CN108192649B (en) | 2018-02-02 | 2018-02-02 | Process system for directly producing hydrogen based on coke oven and control method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108192649B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111718738A (en) * | 2020-06-30 | 2020-09-29 | 葛霖 | Coke oven hydrogen utilization method and system |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002069456A (en) * | 2000-08-31 | 2002-03-08 | Kawasaki Steel Corp | Method for recovering sensible heat of coke oven gas |
| US20050100693A1 (en) * | 2003-11-12 | 2005-05-12 | Mesofuel, Incorporated | Hydrogen generation reactor chamber with reduced coking |
| CN101701703A (en) * | 2009-11-25 | 2010-05-05 | 中冶焦耐工程技术有限公司 | Residual heat utilizing technology of coke oven crude gas |
| CN101850949A (en) * | 2010-06-11 | 2010-10-06 | 大连理工大学 | Method with high purity and high recovery rate for purifying hydrogen gas in coke oven gas |
| CN102517043A (en) * | 2011-11-12 | 2012-06-27 | 太原煤气化股份有限公司 | Method for heating and controlling temperature of coke oven |
| US20150141535A1 (en) * | 2011-09-08 | 2015-05-21 | Expander Energy Inc. | Process for co-producing commercially valuable products from byproducts of fischer-tropsch process for hydrocarbon fuel formulation in a gtl environment |
| JP2016035015A (en) * | 2014-08-04 | 2016-03-17 | Ｊｆｅケミカル株式会社 | Method for refining coke oven gas |
-
2018
- 2018-02-02 CN CN201810104747.XA patent/CN108192649B/en not_active Expired - Fee Related
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002069456A (en) * | 2000-08-31 | 2002-03-08 | Kawasaki Steel Corp | Method for recovering sensible heat of coke oven gas |
| US20050100693A1 (en) * | 2003-11-12 | 2005-05-12 | Mesofuel, Incorporated | Hydrogen generation reactor chamber with reduced coking |
| CN101701703A (en) * | 2009-11-25 | 2010-05-05 | 中冶焦耐工程技术有限公司 | Residual heat utilizing technology of coke oven crude gas |
| CN101850949A (en) * | 2010-06-11 | 2010-10-06 | 大连理工大学 | Method with high purity and high recovery rate for purifying hydrogen gas in coke oven gas |
| US20150141535A1 (en) * | 2011-09-08 | 2015-05-21 | Expander Energy Inc. | Process for co-producing commercially valuable products from byproducts of fischer-tropsch process for hydrocarbon fuel formulation in a gtl environment |
| CN102517043A (en) * | 2011-11-12 | 2012-06-27 | 太原煤气化股份有限公司 | Method for heating and controlling temperature of coke oven |
| JP2016035015A (en) * | 2014-08-04 | 2016-03-17 | Ｊｆｅケミカル株式会社 | Method for refining coke oven gas |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111718738A (en) * | 2020-06-30 | 2020-09-29 | 葛霖 | Coke oven hydrogen utilization method and system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108192649B (en) | 2020-01-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102256894B (en) | Method and device for producing raw synthesis gas | |
| CN101391746B (en) | Small-sized coal gasification hydrogen making method | |
| MX2007001249A (en) | Method and apparatus for producing clean reducing gases from coke oven gas. | |
| CN102712959A (en) | Method for producing direct reduced iron with limited CO2 emissions | |
| EP2346600A2 (en) | Energy-efficient system for generating carbon black, preferably in energetic cooperation with systems for generating silicon dioxide and/or silicon | |
| CN103418360A (en) | Regenerative device and method for desulfurized and denitrified active coke | |
| CN103589462A (en) | Technological method for purifying coal oven gas and recovering chemical products | |
| US20160186992A1 (en) | Direct-fired heating method and facility for implementing same | |
| CN104109545A (en) | Process and device for carbonizing coal in indirect heating and direct gas heating ways | |
| CN101724471A (en) | Method for purifying and recycling benzoid hydrocarbon, ammonia and coal tar from coke-oven gas | |
| CN108192649A (en) | The process system and its control method of hydrogen are directly produced based on coke oven | |
| JP2014528503A (en) | Coke dry quenching with carbon dioxide, including subsequent use of produced carbon monoxide | |
| KR101254977B1 (en) | Apparatus and Method for Treating Coke Oven Gas | |
| CN113214683B (en) | Process and device for preparing high-quality carbon black by cracking shale gas with plasma | |
| MX2014007755A (en) | Biomass syngas purification process under positive pressure for producing oil and system configuration thereof. | |
| CN106947541B (en) | Combined method and system for hydrogen production based on low-rank coal pyrolysis water vapor coke quenching water gas | |
| CN203370558U (en) | Desulfurization and denitrification active coke regeneration device | |
| JP4452617B2 (en) | How to separate hydrogen sulfide from coke oven gas and then get pure sulfur in Claus plant | |
| CN102391892B (en) | Blast furnace gas enrichment apparatus and method | |
| CN105985815A (en) | Method for controlling benzene content of benzene-washed coke oven gas in coke oven gas benzene washing system | |
| JP2013128908A (en) | Gas separation recovery method | |
| CN2780777Y (en) | Cleaning cold and clean coal gas forced circulation cover type bright anealing furnace system | |
| CN203639435U (en) | Device for combining normal temperature/low temperature methanol washing to process crude synthesis gas containing oil | |
| CN102786953B (en) | Coke oven grouped novel bridge pipe crude gas waste heat recovery device | |
| JP2017510710A (en) | Equipment and methods for utilizing electrical energy for iron making from iron oxide minerals |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20200114 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |