CN103480436B - Method for solving large pressure difference of iron-molybdenum catalyst in iron-molybdenum converter - Google Patents
Method for solving large pressure difference of iron-molybdenum catalyst in iron-molybdenum converter Download PDFInfo
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Abstract
The invention relates to a method for solving large pressure difference of an iron-molybdenum catalyst in an iron-molybdenum converter, relates to a method for regenerating the iron-molybdenum catalyst, and is used for solving the problem that the stop treatment needs to be carried out and the treatment speed is low when the pressure difference of the existing iron-molybdenum catalyst is large. According to the method, an iron-molybdenum converting system comprises a heating furnace, the iron-molybdenum converter, a first coke oven gas pipe, a second coke oven gas pipe, a fuel gas pipe and an escape pipe; after coke oven gas is fed in the heating furnace and is heated to 400 DEG C, the coke oven gas is mixed with the coke oven gas in the normally running iron-molybdenum converter together to be fed in the iron-molybdenum converter, so that an iron-molybdenum bed is heated till the hot-spot temperature of the bed is 450-500 DEG C; impurities such as coil tar oil and benzene adhered on the surface of the iron-molybdenum catalyst are melted and move downwards, so that the pressure difference of the catalyst bed is reduced, and then the temperature of the iron-molybdenum catalyst bed is reduced to the level of normal production. The method is performed under the condition that facilities such as equipment, pipelines and valves of a fine desulfurization system are not changed, and the pressure difference of the iron-molybdenum catalyst is reduced without stopping production.
Description
Technical field
The present invention relates to the solution that iron-molybdic catalyst pressure reduction is large.
Background technology
Owing to containing coal tar in oven gas, dust, naphthalene, the impurity such as benzene, through wet desulphurization workshop section, compression section, after the oil strainer of fine de-sulfur and pre-desulfurizer, still can not to tar in oven gas, naphthalene, benzene removes totally, a part of impurity is caused to enter in iron molybdenum converter, tar is adsorbed on catalyst surface, long time integration, iron molybdenum converter inlet outlet pressure differential is increased, the gas resistance that compression conveying fine de-sulfur transforms increases, oven gas compressor load is increased, valve valve block easily damages, system is forced to stop more catalyst changeout and valve valve block, add production cost.In order to make the iron-molybdic catalyst in iron molybdenum converter regenerate, existing method is: adopt passivation, the method for rear activation, that is: after system shutdown, qualified with nitrogen displacement, then increases nitrogen amount at 6000 ~ 8000m
3/ h, iron molybdenum gas from converter outlet sends into torch through blow-down pipe.Iron molybdenum converter inlet temperature controls to allocate instrument air into 250 DEG C time, surely must forbid overtemperature when joining oxygen, and in iron molybdenum groove, Stress control is below 4 kilograms.Assay iron molybdenum groove outlet carbon dioxide increases when reducing again joins oxygen amount, and bed temperature fluctuation absolutely not surpasses 500 DEG C, when bed temperature is evened up and iron molybdenum groove exit gas analysis carbon monoxide and carbon dioxide do not have, judge that passivation is qualified; The qualified rear iron molybdenum bed temperature of passivation drops to 250 DEG C, turns off air valve blank off.Pass into the oven gas after desulfurization, flow is at 6000 ~ 8000m
3/ h, turns off nitrogen.Start to allocate carbon disulfide into after oven gas flow, pressure, temperature stabilization, iron-molybdic catalyst starts activation, treats that bed temperature is evened up, and judges that activation is qualified during outlet concentration of hydrogen sulfide height.The method of this iron-molybdic catalyst regeneration will be carried out under the condition of stopping, and speed is slow, and impact is normally produced.
Summary of the invention
The present invention will solve existing iron-molybdic catalyst pressure reduction greatly also will regenerate under the condition of stopping, slow-footed problem, and solves the large method of iron-molybdic catalyst pressure reduction in iron molybdenum converter.
The method that in solution iron molybdenum converter of the present invention, iron-molybdic catalyst pressure reduction is large is carried out according to the following steps:
One, iron molybdenum conversion system comprises heating furnace, iron molybdenum converter, the first coke oven tracheae, the second coke oven tracheae, fuel gas pipe and blow-down pipe;
Heating furnace is by burner hearth, and flue and coil pipe form; Coil pipe is positioned at burner hearth, and flue is positioned at heating furnace top; Flue arranges butterfly valve; The sidewall of burner hearth is opened a fire door, the bottom of burner hearth arranges fuel gas burner;
The inside of iron molybdenum converter arranges upper and lower two-layer iron-molybdic catalyst bed, arranges oven gas entrance at the top of iron molybdenum converter, and bottom arranges oven gas outlet, and iron molybdenum converter sidewall arranges cold shock oven gas entrance between two-layer iron-molybdic catalyst bed;
First coke oven tracheae is divided into two, one is communicated with the porch of the coil pipe of heating furnace, and the 4th valve is set in the entrance front end of coil pipe (1-3), another is communicated with iron molybdenum converter cold shock oven gas entrance, and the first valve is set on cold shock oven gas pipeline, the outlet of coil pipe is connected with the second coke oven tracheae of the oven gas porch of iron molybdenum converter, and the second valve is set on connecting line, blow-down pipe is set between the second valve and the outlet of coil pipe, installation of relief valve on blow-down pipe; Fuel gas pipe meets the fuel gas burner place of heating furnace burner hearth bottom, and arranges the 3rd valve in porch;
Two, adopt the gas in nitrogen or fuel gas displacement fuel gas pipe, make the O in fuel gas pipe
2volume fraction < 0.5%;
Three, the method for the displacement of employing nitrogen or gravity-flow ventilation makes CO and H in burner hearth
2volume fraction≤0.5%;
Four, close the first valve and the second valve, open atmospheric valve, open the 4th valve and oven gas is passed in the coil pipe of heating furnace, make to be full of oven gas in coil pipe, and through atmospheric valve emptying;
Five, fuel gas is passed into fuel gas pipe, open the 3rd valve, fuel gas is sprayed by the fuel gas burner in burner hearth, and fuel gas is lighted for the oven gas in heat(ing) coil, when the temperature of the exit oven gas of coil pipe reaches 395 ~ 400 DEG C, close atmospheric valve, make a call to the second valve, oven gas is passed into the normal iron molybdenum converter run to mix with the endotracheal oven gas of the second coke oven, after mixing, the temperature of oven gas controls to be 350 ~ 380 DEG C, mixing oven gas enters in the iron-molybdic catalyst bed of iron molybdenum converter, making iron-molybdic catalyst bed be warming up to bed hot(test)-spot temperature with the heating rate of 45 ~ 50 DEG C per hour is 450 ~ 500 DEG C, the oven gas of outflow is exported to next workshop section from the oven gas bottom iron molybdenum converter 2,
Six, when to be down to gauge pressure be below 0.01MPa for the oven gas entrance of iron molybdenum converter and the pressure reduction of outlet, close the 3rd valve, the fire in heating furnace is extinguished; Close the second valve and the 4th valve again, after iron-molybdic catalyst bed temperature is down to 320 ~ 325 DEG C, the situation that iron-molybdic catalyst pressure reduction is large is solved.
When to be increased to gauge pressure be 0.2MPa for the oven gas entrance of iron molybdenum converter and the pressure reduction of outlet, method of the present invention can be adopted, this method is at the equipment not changing fine de-sulfur system, pipeline, carry out in the facility situations such as valve, when not stopping production, light heating furnace, oven gas through heating furnace inner coil pipe is heated up, then with normally produce the oven gas carrying out iron molybdenum converter and mix, making the temperature of iron-molybdic catalyst bed be increased to bed hot(test)-spot temperature is 500 DEG C, at this temperature, stick to the coal tar on iron-molybdic catalyst surface, the impurity such as benzene are melted, move down, the pressure reduction of beds is reduced.Parking number of processes can be greatly reduced by method of the present invention, enhance productivity.
Accompanying drawing explanation
The schematic diagram of the regeneration treatment system of Fig. 1 iron-molybdic catalyst of the present invention.
Fig. 2 is the schematic diagram of heating furnace;
Fig. 3 is the schematic diagram of iron molybdenum converter;
Detailed description of the invention
Detailed description of the invention one: in the iron molybdenum converter of present embodiment, the renovation process of iron-molybdic catalyst carries out according to the following steps:
One, iron molybdenum conversion system comprises heating furnace 1, iron molybdenum converter 2, first coke oven tracheae 3, second coke oven tracheae 4, fuel gas pipe 5 and blow-down pipe 6;
Heating furnace 1 is by burner hearth 1-1, and flue 1-2 and coil pipe 1-3 forms; Coil pipe 1-3 is positioned at burner hearth 1-1, and flue 1-2 is positioned at heating furnace 1 top; Flue 1-2 arranges butterfly valve 1-2-1; The sidewall of burner hearth 1-1 is opened a fire door 1-1-1, the bottom of burner hearth 1-1 arranges fuel gas burner 1-1-2;
The inside of iron molybdenum converter 2 arranges upper and lower two-layer iron-molybdic catalyst bed 2-1, at the top of iron molybdenum converter 2, oven gas entrance 2-2 is set, bottom arranges oven gas outlet 2-3, and iron molybdenum converter 2 sidewall arranges cold shock oven gas entrance 2-4 between two-layer iron-molybdic catalyst bed 2-1;
First coke oven tracheae 3 is divided into two, one is communicated with the entrance of the coil pipe 1-3 of heating furnace 1, and the 4th valve 1-8 is set in the entrance front end of coil pipe (1-3), another is communicated with iron molybdenum converter 2 cold shock oven gas entrance 2-4, and the first valve 1-4 is set on cold shock oven gas pipeline, the outlet of coil pipe 1-3 is connected with the second coke oven tracheae 4 at the oven gas entrance 2-2 place of iron molybdenum converter 2, and the second valve 1-5 is set on connecting line, blow-down pipe 6 is set between the second valve 1-5 and the outlet of coil pipe 1-3, installation of relief valve 1-6 on blow-down pipe 6; Fuel gas pipe 5 meets the fuel gas burner 1-1-2 place of heating furnace burner hearth bottom, and arranges the 3rd valve 1-7 in porch;
Two, adopt the gas in nitrogen or fuel gas displacement fuel gas pipe 5, make the O in fuel gas pipe (5)
2volume fraction < 0.5%;
Three, the method for the displacement of employing nitrogen or gravity-flow ventilation makes CO and H in burner hearth
2volume fraction≤0.5%;
Four, close the first valve 1-4 and the second valve 1-5, open atmospheric valve 1-6, open the 4th valve 1-8 and oven gas is passed in the coil pipe 1-3 of heating furnace 1, make to be full of oven gas in coil pipe 1-3, and through atmospheric valve 1-6 emptying;
Five, fuel gas is passed into fuel gas pipe 5, open the 3rd valve 1-7, fuel gas is made to pass into fuel gas burner 1-1-2 place in burner hearth 1-1, and lighted for the oven gas in heat(ing) coil 1-3, when the temperature of the exit oven gas of coil pipe 1-3 reaches 395 ~ 400 DEG C, close atmospheric valve 1-6, make a call to the second valve 1-5, oven gas is passed into the normal iron molybdenum converter 2 run, and mix with the oven gas in the second coke oven tracheae 4, after mixing, the temperature of oven gas controls to be 350 ~ 380 DEG C, mixing oven gas enters in the iron-molybdic catalyst bed 2-1 of iron molybdenum converter 2, making iron-molybdic catalyst bed 2-1 be warming up to bed hot(test)-spot temperature with the heating rate of 45 ~ 50 DEG C per hour is 450 ~ 500 DEG C, the oven gas of 2-3 outflow is exported to next workshop section from the oven gas bottom iron molybdenum converter 2,
Six, when to be down to gauge pressure be below 0.01MPa to the pressure reduction of oven gas entrance 2-2 and the outlet 2-3 of iron molybdenum converter, close the 3rd valve 1-7, the fire in heating furnace 1 is extinguished; Close the second valve 1-5 and the 4th valve 1-8 again, after iron-molybdic catalyst bed temperature is down to 320 ~ 325 DEG C, the situation that iron-molybdic catalyst pressure reduction is large is solved.
When bed hot(test)-spot temperature in step 5 higher than 500 DEG C time, open the first valve 1-4 quench gas and lower the temperature; In step 6, also can open the first valve 1-4 quench gas and lower the temperature;
Oven gas in first coke oven tracheae 3 and the second coke oven tracheae 4 all comes from pre-desulfurizer.
Detailed description of the invention two: present embodiment and detailed description of the invention one unlike: in step 5, the temperature of the exit oven gas of coil pipe 1-3 is 396 ~ 398 DEG C.Other are identical with detailed description of the invention one.
Detailed description of the invention three: present embodiment mixes with the oven gas in the second coke oven tracheae 4 unlike oven gas being passed in step 5 the iron molybdenum converter 2 normally run with detailed description of the invention one or two, and after mixing, the temperature of oven gas controls to be 360 ~ 370 DEG C.Other is identical with detailed description of the invention one or two.
Detailed description of the invention four: it is 460 ~ 480 DEG C that one of present embodiment and detailed description of the invention one to three are warming up to bed hot(test)-spot temperature unlike iron-molybdic catalyst bed 2-1 in step 5 with the heating rate of 46 ~ 48 DEG C per hour.Other are identical with one of detailed description of the invention one to three.
Detailed description of the invention five: one of present embodiment and detailed description of the invention one to four are 46 ~ 48 DEG C per hour unlike iron-molybdic catalyst bed rate of temperature fall in step 6.Other are identical with detailed description of the invention one.
Beneficial effect of the present invention is verified by following examples
Embodiment 1:(please refer to accompanying drawing 1,2 and 3) renovation process of iron-molybdic catalyst carries out according to the following steps in the iron molybdenum converter of the present embodiment:
Heating furnace 1 is by burner hearth 1-1, and flue 1-2 and coil pipe 1-3 forms; Coil pipe 1-3 is positioned at burner hearth 1-1, and flue 1-2 is positioned at heating furnace 1 top; Flue 1-2 arranges butterfly valve 1-2-1; The sidewall of burner hearth 1-1 is opened a fire door 1-1-1, the bottom of burner hearth 1-1 arranges fuel gas burner 1-1-2;
The inside of iron molybdenum converter 2 arranges upper and lower two-layer iron-molybdic catalyst bed 2-1, at the top of iron molybdenum converter 2, oven gas entrance 2-2 is set, bottom arranges oven gas outlet 2-3, and iron molybdenum converter 2 sidewall arranges cold shock oven gas entrance 2-4 between two-layer iron-molybdic catalyst bed 2-1;
First coke oven tracheae 3 is divided into two, one is communicated with the entrance of the coil pipe 1-3 of heating furnace 1, and the 4th valve 1-8 is set in the entrance front end of coil pipe (1-3), another is communicated with iron molybdenum converter 2 cold shock oven gas entrance 2-4, and the first valve 1-4 is set on cold shock oven gas pipeline, the outlet of coil pipe 1-3 is connected with the second coke oven tracheae 4 at the oven gas entrance 2-2 place of iron molybdenum converter 2, and the second valve 1-5 is set on connecting line, blow-down pipe 6 is set between the second valve 1-5 and the outlet of coil pipe 1-3, installation of relief valve 1-6 on blow-down pipe 6; Fuel gas pipe 5 meets the fuel gas burner 1-1-2 place of heating furnace burner hearth bottom, and arranges the 3rd valve 1-7 in porch;
Two, adopt nitrogen displacement fuel gas pipe 5, work as O
2volume fraction qualified when being 0.5%;
Three, the method for employing gravity-flow ventilation makes CO and H in burner hearth
2volume fraction be 0.5%;
Four, close the first valve 1-4 and the second valve 1-5, open atmospheric valve 1-6, oven gas is passed in the coil pipe 1-3 of heating furnace 1, make to be full of oven gas in coil pipe 1-3, and through atmospheric valve 1-6 emptying;
Five, fuel gas is passed into fuel gas pipe 5, open the 3rd valve 1-7, fuel gas is sprayed by the fuel gas burner 1-1-2 in burner hearth 1-1, and fuel gas is lighted for the oven gas in heat(ing) coil 1-3, when the temperature of the exit oven gas of coil pipe 1-3 reaches 400 DEG C, close atmospheric valve 1-6, make a call to the second valve 1-5, oven gas is passed into the normal iron molybdenum converter 2 run to mix with the oven gas in the second coke oven tracheae 4, after mixing, the temperature of oven gas controls to be 380 DEG C, mixing oven gas enters in the iron-molybdic catalyst bed 2-1 of iron molybdenum converter 2, making iron-molybdic catalyst bed 2-1 be warming up to bed hot(test)-spot temperature with the heating rate of 45 ~ 50 DEG C per hour is 500 DEG C, the oven gas of 2-3 outflow is exported to next workshop section from the oven gas bottom iron molybdenum converter 2, namely ferrimanganic desulfurizer removes inorganic sulfur workshop section,
Six, when to be down to gauge pressure be below 0.01MPa to the pressure reduction of oven gas entrance 2-2 and the outlet 2-3 of iron molybdenum converter, close the 3rd valve 1-7, the fire in heating furnace 1 is extinguished; Close the second valve 1-5 and the 4th valve 1-8 again, after making iron-molybdic catalyst bed temperature be down to 320 ~ 325 DEG C, the situation that iron-molybdic catalyst pressure reduction is large is solved.
Oven gas in first coke oven tracheae 3 of this test and the second coke oven tracheae 4 all comes from pre-desulfurizer.
In this test when bed hot(test)-spot temperature in step 5 higher than 500 DEG C time, open the first valve 1-4 quench gas and lower the temperature;
In the step 6 of this test, open the first valve 1-4 quench gas during cooling, lower the temperature with this;
This test is at the equipment not changing fine de-sulfur system, pipeline, the method that the pressure reduction of the solution iron-molybdic catalyst bed carried out in the facility situations such as valve is large, carry out when the oven gas entrance 2-2 of iron molybdenum converter is 0.4MPa with the pressure reduction of outlet 2-3, through process, it is 0.008MPa that pressure reduction is down to gauge pressure, the method does not affect normal production, need not stop and carry out, in processing procedure, the hot(test)-spot temperature of iron-molybdic catalyst bed is up to 500 DEG C, at this temperature, stick to the coal tar on iron-molybdic catalyst surface, dust, naphthalene, the impurity such as benzene are melted, move down, remove from iron-molybdic catalyst surface, the pressure reduction of beds is reduced, recover catalytic activity, reduce catalyst change number of times, reduce production cost, improve production efficiency.
Claims (5)
1. the solution that in iron molybdenum converter, iron-molybdic catalyst pressure reduction is large, is characterized in that the method is carried out according to the following steps:
One, iron molybdenum conversion system comprises heating furnace (1), iron molybdenum converter (2), the first coke oven tracheae (3), the second coke oven tracheae (4), fuel gas pipe (5) and blow-down pipe (6);
Heating furnace (1) is by burner hearth (1-1), and flue (1-2) and coil pipe (1-3) form; Coil pipe (1-3) is positioned at burner hearth (1-1), and flue (1-2) is positioned at heating furnace (1) top; Flue (1-2) arranges butterfly valve (1-2-1); The sidewall of burner hearth (1-1) is opened a fire door (1-1-1), the bottom of burner hearth (1-1) arranges fuel gas burner (1-1-2);
The inside of iron molybdenum converter (2) arranges upper and lower two-layer iron-molybdic catalyst bed (2-1), at the top of iron molybdenum converter (2), oven gas entrance (2-2) is set, bottom arranges oven gas outlet (2-3), and iron molybdenum converter (2) sidewall arranges cold shock oven gas entrance (2-4) between two-layer iron-molybdic catalyst bed (2-1);
First coke oven tracheae (3) is divided into two, one is communicated with the entrance of the coil pipe (1-3) of heating furnace (1), and the 4th valve (1-8) is set in the entrance front end of coil pipe (1-3), another is communicated with iron molybdenum converter (2) cold shock oven gas entrance (2-4), and the first valve (1-4) is set on cold shock oven gas pipeline, the outlet of coil pipe (1-3) is connected with the second coke oven tracheae (4) at oven gas entrance (2-2) place of iron molybdenum converter (2), and the second valve (1-5) is set on connecting line, blow-down pipe (6) is set between the second valve (1-5) and the outlet of coil pipe (1-3), the upper installation of relief valve (1-6) of blow-down pipe (6), fuel gas pipe (5) meets fuel gas burner (1-1-2) place of heating furnace burner hearth bottom, and arranges the 3rd valve (1-7) in porch,
Two, adopt the gas in nitrogen or fuel gas displacement fuel gas pipe (5), make the volume fraction < 0.5% of the O2 in fuel gas pipe (5);
Three, the method for nitrogen displacement or gravity-flow ventilation is adopted to make volume fraction≤0.5% of CO and H2 in burner hearth;
Four, the first valve (1-4) and the second valve (1-5) is closed, open atmospheric valve (1-6), opening the 4th valve (1-8) passes in the coil pipe (1-3) of heating furnace (1) by oven gas, make to be full of oven gas in coil pipe (1-3), and through atmospheric valve (1-6) emptying;
Five, fuel gas is passed into fuel gas pipe (5), open the 3rd valve (1-7), fuel gas is sprayed by the fuel gas burner (1-1-2) in burner hearth (1-1), and oven gas fuel gas lighted in heat(ing) coil (1-3), when the temperature of the exit oven gas of coil pipe (1-3) reaches 390 ~ 400 DEG C, close atmospheric valve (1-6), make a call to the second valve (1-5), oven gas is passed into the normal iron molybdenum converter (2) run to mix with the oven gas in the second coke oven tracheae (4), after mixing, the temperature of oven gas controls to be 350 ~ 380 DEG C, mixing oven gas enters in the iron-molybdic catalyst bed (2-1) of iron molybdenum converter (2), making iron-molybdic catalyst bed (2-1) be warming up to bed hot(test)-spot temperature with the heating rate of 45 ~ 50 DEG C per hour is 450 ~ 500 DEG C, the oven gas that oven gas outlet (2-3) bottom iron molybdenum converter (2) flows out is to next workshop section,
Six, when to be down to gauge pressure be below 0.01MPa to the pressure reduction of oven gas entrance (2-2) and the outlet (2-3) of iron molybdenum converter, close the 3rd valve (1-7), the fire in heating furnace (1) is extinguished; Close the second valve (1-5) and the 4th valve (1-8) again, after iron-molybdic catalyst bed temperature is down to 320 ~ 325 DEG C, the situation that iron-molybdic catalyst pressure reduction is large is solved.
2. the solution that in iron molybdenum converter according to claim 1, iron-molybdic catalyst pressure reduction is large, is characterized in that the temperature of the exit oven gas of coil pipe in step 5 (1-3) is 396 ~ 398 DEG C.
3. the solution that in iron molybdenum converter according to claim 1 and 2, iron-molybdic catalyst pressure reduction is large, it is characterized in that in step 5, oven gas being passed into the normal iron molybdenum converter (2) run mixes with the oven gas in the second coke oven tracheae (4), after mixing, the temperature of oven gas controls to be 360 ~ 370 DEG C.
4. the solution that in iron molybdenum converter according to claim 1 and 2, iron-molybdic catalyst pressure reduction is large, it is characterized in that in step 5 that iron-molybdic catalyst bed (2-1) is warming up to bed hot(test)-spot temperature with the heating rate of 46 ~ 48 DEG C per hour is 460 ~ 480 DEG C.
5. the solution that in iron molybdenum converter according to claim 1 and 2, iron-molybdic catalyst pressure reduction is large, is characterized in that in step 6, iron-molybdic catalyst bed rate of temperature fall is 46 ~ 48 DEG C per hour.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3764123A (en) * | 1970-06-29 | 1973-10-09 | Midland Ross Corp | Method of and apparatus for reducing iron oxide to metallic iron |
| US4069071A (en) * | 1975-04-11 | 1978-01-17 | Societe Chimique De La Grande Paroisse, Azote Et Produits Chimiques | Method for generating a reducing atmosphere for heat-treating installations |
| CN101134180A (en) * | 2007-10-11 | 2008-03-05 | 广西大学 | High iron pelitization wulfenite floatation method |
| CN101704712A (en) * | 2009-10-29 | 2010-05-12 | 山西焦化股份有限公司 | Technological method for preparing methanol by combining coke oven gas with water gas |
-
2013
- 2013-10-21 CN CN201310494794.7A patent/CN103480436B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3764123A (en) * | 1970-06-29 | 1973-10-09 | Midland Ross Corp | Method of and apparatus for reducing iron oxide to metallic iron |
| US4069071A (en) * | 1975-04-11 | 1978-01-17 | Societe Chimique De La Grande Paroisse, Azote Et Produits Chimiques | Method for generating a reducing atmosphere for heat-treating installations |
| CN101134180A (en) * | 2007-10-11 | 2008-03-05 | 广西大学 | High iron pelitization wulfenite floatation method |
| CN101704712A (en) * | 2009-10-29 | 2010-05-12 | 山西焦化股份有限公司 | Technological method for preparing methanol by combining coke oven gas with water gas |
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