CN1394965A - Melt reduction iron-smelting dimethyl ether production and power generation combined production method and installation - Google Patents
Melt reduction iron-smelting dimethyl ether production and power generation combined production method and installation Download PDFInfo
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- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 title claims abstract description 204
- 238000003723 Smelting Methods 0.000 title claims abstract description 52
- 238000010248 power generation Methods 0.000 title claims abstract description 37
- 230000009467 reduction Effects 0.000 title claims description 62
- 238000004519 manufacturing process Methods 0.000 title claims description 41
- 238000009434 installation Methods 0.000 title 1
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 70
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 68
- 239000007789 gas Substances 0.000 claims abstract description 49
- 238000000034 method Methods 0.000 claims abstract description 48
- 239000003054 catalyst Substances 0.000 claims abstract description 39
- 230000008569 process Effects 0.000 claims abstract description 38
- 239000002002 slurry Substances 0.000 claims abstract description 32
- 239000012442 inert solvent Substances 0.000 claims abstract description 22
- 238000000926 separation method Methods 0.000 claims abstract description 9
- 239000002918 waste heat Substances 0.000 claims abstract description 6
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 92
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 81
- 229910052742 iron Inorganic materials 0.000 claims description 46
- 239000003034 coal gas Substances 0.000 claims description 28
- 238000000746 purification Methods 0.000 claims description 24
- 239000000047 product Substances 0.000 claims description 23
- 238000010521 absorption reaction Methods 0.000 claims description 19
- 239000002994 raw material Substances 0.000 claims description 18
- 238000005262 decarbonization Methods 0.000 claims description 11
- 239000000428 dust Substances 0.000 claims description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 238000006297 dehydration reaction Methods 0.000 claims description 8
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 7
- 239000003245 coal Substances 0.000 claims description 7
- 229910052802 copper Inorganic materials 0.000 claims description 7
- 239000010949 copper Substances 0.000 claims description 7
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- 239000007788 liquid Substances 0.000 claims description 6
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- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 239000000843 powder Substances 0.000 claims description 4
- 238000003860 storage Methods 0.000 claims description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 3
- 230000009471 action Effects 0.000 claims description 3
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 3
- 239000006227 byproduct Substances 0.000 claims description 3
- 229910052593 corundum Inorganic materials 0.000 claims description 3
- 238000005516 engineering process Methods 0.000 claims description 3
- 229940057995 liquid paraffin Drugs 0.000 claims description 3
- 239000002480 mineral oil Substances 0.000 claims description 3
- 235000010446 mineral oil Nutrition 0.000 claims description 3
- 229910001845 yogo sapphire Inorganic materials 0.000 claims description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 2
- 235000019738 Limestone Nutrition 0.000 claims description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 2
- WUKWITHWXAAZEY-UHFFFAOYSA-L calcium difluoride Chemical compound [F-].[F-].[Ca+2] WUKWITHWXAAZEY-UHFFFAOYSA-L 0.000 claims description 2
- 230000023556 desulfurization Effects 0.000 claims description 2
- 238000010702 ether synthesis reaction Methods 0.000 claims description 2
- 239000010436 fluorite Substances 0.000 claims description 2
- 238000010438 heat treatment Methods 0.000 claims description 2
- 239000006028 limestone Substances 0.000 claims description 2
- 239000002808 molecular sieve Substances 0.000 claims description 2
- 239000008188 pellet Substances 0.000 claims description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical group [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 2
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- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- DHZBEENLJMYSHQ-XCVPVQRUSA-N cantharidin Chemical compound C([C@@H]1O2)C[C@@H]2[C@]2(C)[C@@]1(C)C(=O)OC2=O DHZBEENLJMYSHQ-XCVPVQRUSA-N 0.000 description 1
- DHZBEENLJMYSHQ-UHFFFAOYSA-N cantharidine Natural products O1C2CCC1C1(C)C2(C)C(=O)OC1=O DHZBEENLJMYSHQ-UHFFFAOYSA-N 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
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Abstract
The present invention relates to a method which adopts the gas produced in the melt reducing iron-smelting process, through the processes of heat exchange, dust-removing, desulfuration, pressurizing, adding catalyst and inert solvent and utilizing slurry bed reactor to produce dimethyl ether and utilizes waste heat to make power generation. Said system method includes melt reducing iron-smelting equipment, synthesis gas cleaning equipment, dimethyl ether synthesijs equipment, product separation equipment and power generator equipment.
Description
Technical Field
The invention belongs to the fields of metallurgy, chemical industry and energy, and particularly relates to smelting reduction iron making, dimethyl ether production and power generation by utilizing waste heat.
Background
Smelting reduction is an advanced ironmaking process technology, which not only can solve the two problems of increasingly deficient coke and environmental pollution in the current steel industry, but also greatly shortens the process flow, improves the productivity, reduces the capital investment and the production cost and increases the production flexibility because of omitting the coking and sintering processes (ZL99122119.2, ZL99122120.6, ZL99122121.4 and ZL 00238120.6). When molten iron is produced by the smelting reduction iron-making process, a large amount of coal gaswith high calorific value is also produced as a byproduct. How to utilize the coal gas and the related waste heat to achieve the purpose of comprehensive co-production is a subject which is always sought by people. While the austempered steel coupling utilizes the coal gas in the smelting reduction process to produce the sponge iron, the assumption that the coal gas in the smelting reduction ironmaking process is utilized to synthesize chemical raw materials is also proposed; the technical idea of clean power generation using process gas from smelting reduction iron making has been proposed in japan, but both of them have not been proposed and implemented.
Disclosure of Invention
The invention aims to provide a high-efficiency, environment-friendly and energy-saving co-production method and device combining smelting reduction ironmaking, dimethyl ether production and power generation based on smelting reduction ironmaking.
In order to solve the above problems, the combined production method combining smelting reduction iron making, dimethyl ether production and power generation is based on smelting reduction iron making, takes the coal gas in the smelting reduction process as a main raw material, and is added with relevant catalysts and inert solvents to produce dimethyl ether in a dimethyl ether synthesis device, and utilizes the steam generated by the heat exchange of the coal gas generated in the smelting reduction iron making process through a heat exchanger and the residual heat generated in the dimethyl ether production process to enter a steam bag to generate steam for power generation. Now, as to the technical solution, the detailed description will be given,
(1) the smelting reduction iron-making uses iron ore, iron ore powder and pellets, lump coal and coal powder thereof as main raw materials, uses industrial pure oxygen or low-purity oxygen, limestone, fluorite and the like as auxiliary raw materials, adopts a two-step smelting reduction iron-making technology of pre-reduction and final reduction to produce molten iron, and simultaneously produces a large amount of coal gas with high calorific value in the molten iron production process, wherein the coal gas amount can reach 1300-2300 Nm3The calorific value of coal gas can reach 6000 to 8500KJ/Nm per ton of molten iron3。
(2) High heating value coal gas generated in the smelting reduction iron-making process is taken as a main raw material and is introduced into a furnace
In the slurry bed reactor of dimethyl ether synthesis device of catalyst and inert solvent
Carrying out dimethyl ether synthesis reaction under the action of the catalyst, and obtaining a synthetic product after absorption, decarburization and rectification
To obtain the high-concentration dimethyl ether.
The proportion (weight percent) of the catalyst and the inert solvent in the raw materials for synthesizing the dimethyl ether is as follows:
5-45% of catalyst and 55-95% of inert solvent.
The main components of the coal gas are as follows: CO 30-75%, H27～8％、CO 23～32％；
The airspeed of the coal gas is 1500-10000 h-1；
Hot coal gas generated in the smelting reduction iron-making process of raw materials is subjected to heat exchange, dust removal, fine desulfurization and pressurization treatment, and then is used as a raw material to enter a dimethyl ether synthesis device. The gas pressure is 2.0-8.0 MPa.
The catalyst in the raw materials adopts a copper-based methanol synthesis catalyst and a methanol dehydration catalyst, and the weight ratio of the copper-based methanol synthesis catalyst to the methanol dehydration catalyst is 0.5-4.
The copper-based methanol synthesis catalyst is any one of C301, C302, C306 or C207.
The methanol dehydration catalyst is molecular sieve ZSM-5 or gama-Al2O3Any of the above.
The inert solvent in the raw materials is any one of liquid paraffin, mineral oil, cantharidine, alcohol or ether containing 18-35 carbon chains, chloralkane, aromatic hydrocarbon and derivatives thereof in alkane solvents.
The technological parameters of the dimethyl ether synthesis process are as follows:
the working temperature is 200-320 ℃;
the working pressure is 2.0-8.0 MPa;
the dimethyl ether synthesis process is a water gas shift reaction, a methanol synthesis reaction and a methanol dehydration reaction coupling process, namely, three reactions are simultaneously carried out in a slurry bed reactor, namely:
the product obtained after the synthesis reaction contains dimethyl ether (CH)3OCH3) Methanol (CH)3OH), water (H)2O), unreacted H2、CO、CO2And part of catalyst and inert solvent carried by the substances enter a primary separator from the top of a slurry bed reactor of the dimethyl ether synthesis device for separation, the inert solvent and the catalyst are separated from a gaseousproduct, the gaseous product enters an absorption tower, and dimethyl ether, methanol, water and part of CO are carried by the gaseous product2The absorbed liquid phase enters a decarbonizing tower to remove CO2And the rest product enters a dimethyl ether rectifying tower for rectification. The unabsorbed gas species are returned to the compressor to join the feed gas.
The absorption parameters of the absorption tower are as follows:
gas inlet temperature: -10 to 40 DEG C
Liquid inlet temperature: 10-60 DEG C
The pressure in the tower is as follows: 1.0 to 3.0MPa,
decarburization parameters of a decarburization tower
Liquid inlet temperature: 150-210 DEG C
Temperature at the outlet of the column bottom: 180-220 deg.C
The pressure in the tower is as follows: 1.0 to 2.0MPa,
then the dimethyl ether enters a dimethyl ether rectifying tower for rectification, and the dimethyl ether rectifying parameters are
Liquid inlet temperature: 180 to 200 DEG C
Temperature at the outlet of the column bottom: 180-220 deg.C
The pressure in the tower is as follows: 0.6 to 1.5 MPa.
After rectification, high-concentration dimethyl ether can be obtained.
In the rectification process, the distillate at the tower bottom is methanol and water, part of the distillate is used as a raw material and returns to the slurry bed reactor and is used as an absorbent and returns to the absorption tower, and the rest is rectified to recover the methanol.
(3) Steam generated by heat exchange of coal gas in the smelting reduction iron-making process through a heat exchanger and steam generated in the dimethyl ether synthesis process respectively enter a steam pocket of a power generation device, and the steam is used as power to drive a steam turbine or other power generation devices to generate power. The steam parameters for power generation were:
the steam pressure is 1-7 Mpa
The steam temperature is 130-300 ℃.
The invention relates to a combined production device combining smelting reduction ironmaking, dimethyl ether production and power generation, which consists of a smelting reduction ironmaking device, a synthetic gas purification device, a dimethyl ether synthesis device, a product separation device and a power generation device.
The co-production apparatus of the present invention combining smelting reduction iron making, dimethyl ether production and power generation will now be described in detail with reference to the accompanying drawings.
Drawings
FIG. 1 is a schematic structural diagram of a combined production device combining smelting reduction iron making, dimethyl ether production and power generation.
As seen from fig. 1, the combined production apparatus of smelting reduction iron making, dimethyl ether production and power generation of the present invention is composed of a smelting reduction iron making apparatus S1, a synthesis gas purification apparatus S2, a dimethyl ether synthesis apparatus S3, a product separation apparatus S4 and a power generation apparatus S5, all of which are enclosed by dashed lines.
The devices and their connections are now described as follows:
① A smelting reduction ironmaking apparatus S1 is composed of a pre-reduction furnace 04, a final reduction furnace 11, bins 01 and 02, dust collectors 06 and 15, a blanking pipe 10 and its related pipes 05, 07, 08, 09, 14 and 16, and in the final reduction furnace 11, there are an oxidation conveying pipe 03, a tapping hole 13 and a slag hole 12.
The pre-reduction furnace 04 is connected with the final reduction furnace 11 through a blanking pipe 10, the pre-reduction furnace 04 is connected with a dust remover 06 through a pipeline 05, the final reduction furnace 11 is connected with a dust remover 15 through a pipeline 14, the dust remover 15 is connected with the pre-reduction furnace through a pipeline 16, and the dust remover 06 is further connected with the final reduction furnace 11 through a pipeline 07. The entire smelting reduction iron making apparatus S1 is connected to the syngas cleaning apparatus S2 through a pipe 08.
② A synthetic gas purification device S2 is composed of a heat exchanger 17, a synthetic gas purification tower 19, a compressor 21 and related pipelines 18, 20, 22, 23, wherein the heat exchanger 17 is connected with a dust remover 06 of a smelting reduction iron making device S1 through pipelines 08, 09 and is connected with the synthetic gas purification tower 19 through a pipeline 18, the synthetic gas purification tower 19 is connected with the compressor 21 through a pipeline 20, and the heat exchanger 17 is connected with a steam bag 45 of a power generation device S5 through a pipeline 23.
③ dimethyl ether synthesis device S3 is composed of heat exchanger 24, slurry bed reactor 26, primary separator 28 and related pipelines 25, 27, 29, 31, 32, 43, the heat exchanger 24 is connected with compressor 21 in synthesis gas purification device S2 through pipeline 22 and is connected with slurry bed reactor 26 through pipeline 25, slurry bed reactor 26 is connected with primary separator 28 through pipelines 27, 29, primary separator 28 is connected with heat exchanger 24 through pipeline 31, slurry bed reactor 26 is connected with steam bag 45 of power generation device S5 through pipeline 47, 30 on top of slurry bed reactor 26 is the inlet for catalyst and inert solvent;
④ product separation device S4 is composed of absorption tower 33, decarbonization tower 37, dimethyl ether rectification tower 39, dimethyl ether storage tank 42 and corresponding pipelines 34, 35, 36, 41 and 49, wherein the absorption tower 33 is connected with the slurry bed reactor 26 in the dimethyl ether synthesis device S3 through pipelines 36 and 43 and is connected with the decarbonization tower 37 through a pipeline 35, the absorption tower 33 is also connected with the heat exchanger 24 in the dimethyl ether synthesis device S3 through a pipeline 32 and is connected with the compressor 21 of the synthesis gas purification device S2 through a pipeline 34, the decarbonization tower 37 is connected with the dimethyl ether rectification tower 39 through a pipeline 49, the top of the decarbonization tower 37 is provided with a non-condensable gas outlet 38, the top of the dimethyl ether rectification tower 39 is connected with the dimethyl ether rectification tank 42 through a pipeline 41, the bottom of the tower is provided with an outlet 40, and is connected with the slurry bed reactor 26 through a pipeline 43.
⑤ the power generation device S5 is composed of a steam bag 45, a generator 48 and a pipeline 46, the steam bag 45 is also connected with the heat exchanger 17 of the synthesis gas purification device S2 and the slurry bed reactor 26 of the dimethyl ether synthesis device S3 through pipelines 23 and 47 respectively;
in the whole combined production device combining smelting reduction ironmaking, dimethyl ether production and power generation, a smelting reduction ironmaking device S1 is connected with a synthesis gas purification device S2 through a pipeline 08, a synthesis gas purification device S2 is connected with a dimethyl ether synthesis device S3 and a power generation device S5 through pipelines 22 and 23 respectively, and a dimethyl ether synthesis device S3 is connected with a product separation device S4 and a power generation device S5 through pipelines 32 and 47 respectively.
According to the method and the device, the combined production process of smelting reduction iron making, dimethyl ether production and power generation is as follows:
firstly, the smelting reduction iron-making device S1 of the invention is adopted to produce molten iron by a conventional two-step method, and when the molten iron is produced, a large amount of coal gas generated in the pre-reduction furnace 04 is dedusted by the deduster 06, enters the heat exchanger 17 of the synthesis gas purification device S2 to exchange heat and reduce temperature, and then enters the synthesis gas purification tower 19 to further dedust and desulfurize. The dust is removed, desulfurized and compressed by a compressor 21, enters a heat exchanger 24 in a dimethyl ether synthesis device S3, and has certain pressure after heat exchangeThe coal gas (synthesis gas) enters a slurry bed reactor 26, at the moment, the catalyst and the inert solvent are also added into the slurry bed reactor 26 from an inlet 30, the three react in the slurry bed reactor 26, and the product obtained after the reaction comprises dimethyl ether, methanol, water and unreacted H2、CO、CO2And entrained catalyst and inert solvent, these products enter the initial separator 28 from the top of the slurry bed reactor 26 through the pipeline 27, separate inert solvent and catalyst from gaseous products, and return to the slurry bed reactor 26 through the pipeline 29, the gaseous products reenter the heat exchanger 24 through the pipeline 31 for heat exchange, enter the absorption tower 33 through the pipeline 32, after absorption by the absorption tower 33, H in the mixed product2、CO、CO2The gas phase is still in the gas phase and returns to the compressor 21 through a pipeline 34 to be mixed with fresh coal gas (synthesis gas) for recycling or directly used as waste heat for recycling; and dimethyl ether, methanol, water and a small amount of CO2Is in liquid phase and is fed via line 35 to a decarbonation column 37 where after decarbonation, CO is obtained2Separated from the tower top 38, the distillate at the bottom of the decarbonizing tower 38 enters a dimethyl ether rectifying tower 37 through a pipeline 35 for rectification, and the rectified high-concentration dimethyl ether product is led out from an outlet 41 at the tower top and is sent to a dimethyl ether storage tank 42 for storage after being cooled; the distillate at the bottom of the rectifying tower 39 is methanol and water, part of the distillate is sent to the slurry bed reactor 26 and the absorption tower 33 through the outlet 40 by pipelines 43 and 36, and the rest enters the methanol rectifying tower by a pipeline 44 to recover the methanol.
In addition, steam generated when coal gas generated in the iron making process of the smelting reduction iron making device S1 exchanges heat through the heat exchanger 17 enters the steam pocket 45 in the power generation device S5 through the pipeline 23, waste heat generated in the dimethyl ether synthesis process also enters the steam pocket through the pipeline 47 to convert the steam, and the two streams of steam are merged and enter the turbine generator 48 to generate power.
Therefore, the purposes of smelting reduction iron making, dimethyl ether production and power generation co-production are achieved.
Compared with the prior art, the invention has the following advantages:
① the coal gas generated in the melting reduction process is a CO-rich synthetic gas, wherein the CO content is 30-75%，H2The content of the dimethyl ether is 7-8%, and the tower bottom distillate (mainly methanol and water) after dimethyl ether rectification can be fed into the slurry bed reactor 26 again through a pipeline 43 to adjust the hydrogen-carbon ratio and improve the productivity of dimethyl ether and the CO conversion rate.
② in the slurry bed reactor 26, CO/H2Wide, CO content up to 30-75%, CO2The concentration range is large (3-32%), so the dimethyl ether synthesis process has large operation flexibility and convenient work.
③ because of the dimethyl ether synthesis process, when adopting the once-through process, the CO conversion reaches 85%, and when adopting the low-circulation process, the CO conversion rate reaches 70%, which is obviously higher than the CO conversion rate (usually lower than 10%) in the traditional methanol synthesis process.
④ the invention aims at the best conversion effect of energy and resources in the co-production process (integrated process), utilizes the primary conversion of carbon in coal to complete the reduction process of iron in iron-containing raw materials, and then utilizes the byproduct gas to further convert and synthesize dimethyl ether, thus achieving the purpose of system optimization (minimum consumption, minimum waste discharge, etc.), finding a reasonable utilization way for a large amount of tail gas generated by the traditional smelting reduction iron-making process, and solving the problem of main raw materials required by the dimethyl ether synthesis process.
⑤ has low investment, high energy utilization rate, low energy consumption and low cost, and is environment friendly.
Examples
Three batches of experiments are carried out by adopting the co-production method and the device for combining smelting reduction iron making, dimethyl ether production and power generation.
Firstly, raw materials such as ores, fluxes, coal and the like and oxygen are respectively fed into a melting reduction device from bins 01 and 02 and an oxygen conveying pipe 03 according to a certain proportion for iron making, and molten iron is discharged from a molten iron outlet 13. Simultaneously, a large amount of coal gas is generated. The gas composition, gas generation amount and iron yield are shown in table 1. The produced gas is dedusted by dedusters 06, 15, heat exchanged by a heat exchanger 17, dedusted and desulfurized by a synthesis gas purification tower 19, and compressed by a compressor 21 to have a certain pressure to enter from the bottom of a slurry bed reactor 26 in a dimethyl ether synthesis device S3, a catalyst and an inert solvent are added from an inlet 30 in advance, and the inert solvent, the components of the catalyst and the weight ratio thereof are shown in Table 2. In the slurry bed reactor 26, the coal gas is used for dimethyl ether synthesis under the action of the catalyst and the inert solvent, and the technological parameters of the synthesis process are listed in the table 3. The synthesized product is decarbonized by a decarbonization tower 33 and rectified by a dimethyl ether rectifying tower 39, and high-concentration dimethyl ether is obtained after rectification. The decarburization and rectification parameters are shown in Table 4. The indices of the obtained 3 batches of dimethyl ether are shown in Table 5.
In the above process, the steam generated by the heat exchange of the coal gas generated by the smeltingreduction iron making through the heat exchanger and the residual heat generated in the dimethyl ether synthesis process enter the steam bag to convert the steam, the steam pressure and the steam temperature are listed in table 6.
TABLE 1 examples gas composition, gas generation amount and iron production amount
| Batch number | Amount of iron produced t/h | Gas composition% vol | Gas generation amount Nm3T molten iron | |||
| CO | CO2 | N2 | H2 | |||
| 1 | 3 | 62～75 | 8～14 | 2～5 | 7～14 | 1900 |
| 2 | 3.5 | 40～48 | 23～32 | 2～5 | 10～18 | 1340 |
| 3 | 3.3 | 52～59 | 19～25 | 2～5 | 8～15 | 1670 |
TABLE 2 examples catalyst and inert solvent ratio (by weight) in dimethyl ether synthesis
| Batch number | Catalyst and process for preparing same | Inert solvent | ||||
| Copper-based methanol synthesis catalyst | | |||||
| 1 |
| 20 | ZSM-5 | 10 | Liquid paraffin | 570 |
| 2 | C302 | 50 | gama-Al2O3 | 50 | Mineral oil | 400 |
| 3 |
| 20 | ZSM-5 | 5 | Kexarane | 220 |
Table 3 examples synthesis process parameters of dimethyl ether in the synthesis plant
| Batch number | Working temperature/. degree.C | Working pressure/MPa | Space velocity/h of |
| 1 | 220 | 3 | 2500 |
| 2 | 270 | 5 | 6000 |
| 3 | 270 | 8 | 9000 |
Table 4 absorption, decarbonisation and dimethyl ether rectification parameters of the products of the synthesis of the examples
| Batch number | Decarburization parameter | Decarburization parameter | Rectification parameter of dimethyl ether | ||||||
| Inlet port Temperature of ℃ | An outlet Temperature of ℃ | Pressure of MPa | Inlet port Temperature of ℃ | An outlet Temperature of ℃ | Pressure of MPa | Inlet port Temperature of ℃ | An outlet Temperature of ℃ | Pressure of
| |
| 1 | 15 | 45 | 2.0 | 170 | 210 | 2.0 | 130 | 160 | 0.6 |
| 2 | 32 | 16 | 1.3 | 180 | 200 | 1.5 | 150 | 170 | 0.8 |
| 3 | 2 | 32 | 1.6 | 160 | 190 | 1.2 | 170 | 190 | 1.2 |
Table 5 indication of the dimethyl ether product obtained in the examples
| Batch number | Index of |
| 1 | The content of dimethyl ether is more than or equal to 99.5 |
| 2 | The content of dimethyl ether is more than or equal to 99.98 |
| 3 | The content of dimethyl ether is more than or equal to 95 percent |
Table 6 steam pressure and steam temperature for steam drum of example
| Batch number | Steam pressure MPa | Temperature of |
| 1 | 4.0 | 220 |
| 2 | 5.5 | 175 |
| 3 | 3.2 | 205 |
Claims (10)
1. A combined production method combining smelting reduction iron making, dimethyl ether production and power generation comprises smelting reduction iron making, namely iron ore, iron ore powder and pellets, lump coal and coal powder are used as main raw materials, industrial pure oxygen or low-purity oxygen, limestone, fluorite and the like are used as auxiliary raw materials, a pre-reduction and final reduction two-step smelting reduction iron making technology is adopted to produce molten iron, meanwhile, in the smelting reduction iron making process, a large amount of coal gas with high calorific value is also produced as a byproduct, and the combined production method is characterized in that:
① high-calorific-value coal gas generated in smelting reduction iron-making process is used as main raw material, and is added with
In a slurry bed reactor of a dimethyl ether synthesis device of catalyst and inert solvent, in the presence of catalyst
The dimethyl ether synthesis reaction is carried out under the action of the catalyst, and after the synthetic product is absorbed, decarbonized and rectified,
so as to obtain the dimethyl ether with high concentration,
the proportion (weight percent) of the catalyst and the inert solvent is as follows:
5-45% of catalyst, 55-95% of inert solvent,
the main components of the coal gas are 30-75% of CO and H27～8％、CO23～32％；
The airspeed of the coal gas is 1500-10000 h-1；
② the process parameters of the dimethyl ether synthesis process are as follows:
the working temperature is 200-320 DEG C
The working pressure is 2.0-8.0 MPa;
③ the parameters of further absorption, decarburization and rectification of the synthetic product obtained in the dimethyl ether synthesis device are respectively:
absorption parameters of absorption tower
Gas inlet temperature: -10 to 40 DEG C
Liquid inlet temperature: 10-60 DEG C
The pressure in the tower is as follows: 1.0-3.0 Mpa, decarbonization parameter of decarbonization tower
Liquid inlet temperature: 150-210 DEG C
Temperature at the outlet of the column bottom: 180-220 deg.C
The pressure in the tower is as follows: 1.0-2.0 MPa, and then entering a dimethyl ether rectification tower for rectification, wherein the dimethyl ether rectification parameters
Liquid inlet temperature: 180 to 200 DEG C
Temperature at the outlet of the column bottom: 180-220 deg.C
The pressure in the tower is as follows: 0.6 to 1.5 MPa.
2. A combined production method combining smelting reduction iron making, dimethyl ether production and power generation is characterized in that: the method is characterized in that water vapor generated by heat exchange of coal gas generated in the smelting reduction iron-making process through a heat exchanger and water vapor obtained by enabling waste heat generated in the dimethyl ether synthesis process to enter a steam packet are used as power and enter a steam turbine to drive a generator to generate electricity, and the steam parameters for generating electricity are as follows:
the steam pressure is 1-7 Mpa, and the steam temperature is 130-300 ℃.
3. The method according to claim 1, wherein the catalyst comprises a copper-based methanol synthesis catalyst and a methanol dehydration catalyst, and the weight ratio of the copper-based methanol synthesis catalyst to the methanol dehydration catalyst is 0.5-4.
4. A process according to claim 1, 3, characterized in that the copper-based methanol synthesis catalyst is any one of C301, C302, C306 or C207.
5. The method of claims 1 and 3, wherein the methanol dehydration catalyst is molecular sieve ZSM-5 or gama-Al2O3Any of the above.
6. The method according to claim 1, wherein the inert solvent is any one of liquid paraffin, mineral oil, canthal, alcohol or ether containing 18 to 35 carbon chains, chlorinated alkane, aromatic hydrocarbon and derivatives thereof in an alkane solvent.
7. The method according to claim 1, characterized in that high heating value coal gas generated in the smelting reduction iron making process is subjected to heat exchange, dust removal, fine desulfurization, deoxidation and pressurization treatment, and then is used as a raw material to enter a dimethyl ether synthesis device.
8. The method according to claims 1 and 7, characterized in that the pressure of the coal gas entering the dimethyl ether synthesis device is 2.0-8.0 MPa.
9. A combined production apparatus combining smelting reduction iron making, dimethyl ether production and power generation, comprising a smelting reduction iron making apparatus (S1), characterized in that:
the device also comprises a synthesis gas purification device (S2), a dimethyl ether synthesis device (S3), a product separation device (S4) and a power generation device (S5); wherein:
① the synthetic gas purification device (S2) is composed of a heat exchanger (17), a synthetic gas purification tower (19), a compressor (21) and related pipelines (18, 20, 22, 23), wherein the heat exchanger (17) is connected with a dust remover (06) of the smelting reduction iron-making device (S1) through pipelines (08, 09) and is connected with the synthetic gas purification tower (19) through the pipeline (18), the synthetic gas purification tower (19) is connected with the compressor (21) through the pipeline (20), and the heat exchanger (17) is connected with a steam packet (45) of the power generation device (S5) through the pipeline (23);
② dimethyl ether synthesis device (S3) is composed of heat exchanger (24), slurry bed reactor (26), primary separator (28) and related pipelines (25, 27, 29, 31, 32, 43), the heat exchanger (24) is connected with compressor (21) in synthesis gas purification device (S2) through pipeline (22) and is connected with slurry bed reactor (26) through pipeline (25), slurry bed reactor (26) is connected with primary separator (28) through pipelines (27, 29), primary separator (28) is connected with heat exchanger (24) through pipeline (31), slurry bed reactor (26) is connected with steam bag (45) of power generation device (S5) through pipeline (47), and top (30) of slurry bed reactor 26 is the feeding inlet of catalyst and inert solvent;
③ product separation device (S4) is composed of an absorption tower (33), a decarbonization tower (37), a dimethyl ether rectification tower (39), a dimethyl ether storage tank (42) and corresponding pipelines (34, 35, 36), wherein the absorption tower (33) is connected with a slurry bed reactor (26) in the dimethyl ether synthesis device (S3) through pipelines (36, 43) and is connected with the decarbonization tower (37) through a pipeline (35), the absorption tower (33) is also connected with a heat exchanger (24) in the dimethyl ether synthesis device (S3) through a pipeline (32) and is connected with a compressor (21) of a synthesis gas purification device (S2) through a pipeline (34), the decarbonization tower (37) is connected with the dimethyl ether rectification tower (39) through a pipeline (49), the top of the decarbonization tower (37) is provided with a noncondensable gas outlet (38), the top of the dimethyl ether rectification tower (39) is connected with the dimethyl ether rectification tank (42) through a pipeline (41), and is provided with an outlet (40) and is connected with the slurry bed reactor (26) through a pipeline (43);
④ power generation facility (S5) is composed of steam bag (45), generator (48) and pipeline (46), the steam bag (45) is also connected with the heat exchanger (17) of the synthesis gas purification facility (S2) and the slurry bed reactor (26) of the dimethyl ether synthesis facility (S3) through pipeline (23) and pipeline (47) respectively;
in the whole combined production device combining smelting reduction ironmaking, dimethyl ether production and power generation, a smelting reduction ironmaking device (S1) is connected with a synthesis gas purification device (S2) through a pipeline (08), the synthesis gas purification device (S2) is respectively connected with a dimethyl ether synthesis device (S3) and a power generation device (S5) through pipelines (22) and (23), and a dimethyl ether synthesis device (S3) is respectively connected with a product separation device (S4) and the power generation device (S5) through pipelines (32) and (47).
10. The apparatus of claim 9, wherein the generator (48) is a turbine generator or other generator.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101219929B (en) * | 2007-01-10 | 2011-03-16 | 中冶赛迪工程技术股份有限公司 | Method and device for producing methanol with COREX fusion reduction furnace coal gas |
| CN106045824A (en) * | 2016-07-28 | 2016-10-26 | 鹤壁宝发能源科技股份有限公司 | Dimethyl ether production system with waste heat electricity generating function and production process |
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2002
- 2002-08-16 CN CN 02128858 patent/CN1239249C/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101219929B (en) * | 2007-01-10 | 2011-03-16 | 中冶赛迪工程技术股份有限公司 | Method and device for producing methanol with COREX fusion reduction furnace coal gas |
| CN106045824A (en) * | 2016-07-28 | 2016-10-26 | 鹤壁宝发能源科技股份有限公司 | Dimethyl ether production system with waste heat electricity generating function and production process |
| CN106045824B (en) * | 2016-07-28 | 2019-02-22 | 鹤壁宝发能源科技股份有限公司 | A kind of dimethyl ether production system and production technology with cogeneration |
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