CN103031154A - Method and device for preparing synthesis gas or hydrogen by direct connection of non-catalytic partial oxidation furnace with BGL gasifier or crushed coal pressurized slag gasifier - Google Patents
Method and device for preparing synthesis gas or hydrogen by direct connection of non-catalytic partial oxidation furnace with BGL gasifier or crushed coal pressurized slag gasifier Download PDFInfo
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Abstract
The invention discloses a method for preparing synthesis gas or hydrogen by direct connection of non-catalytic partial oxidation furnace with a BGL gasifier or a crushed coal pressurized slag gasifier, which takes lump coal as raw material, pure oxygen as oxidizing agent and steam as gasifying agent; the gas at an outlet of the BGL gasifier directly enters the pure oxygen non-catalytic partial oxidation (POX) reformer furnace, and is rapidly mixed with pure oxygen and steam in the POX reformer furnace for burning; and when the temperature is higher than 1300 DEG C, organic matter is cracked at the high temperature and is transformed into high-temperature gas with more than 1300 DEG C. By adopting the POX reformer furnace to replace a washing and cooling separator device arranged on a gasification station of the BGL, the invention does not produce oil-containing gas liquor, so that the problem of environmental pollution caused by the BGL gasification method can be thoroughly solved, and the environmental protection investment is greatly saved. Furthermore, high-temperature combustion of the POX reformer furnace is adopted, so that the product is completely transformed into useful components or simple substances which can be easily removed and treated. For example, methane and light oil are transformed into medium hydrogen and carbon monoxide; and thiophene is transformed into hydrogen sulfide, and the like. The invention also discloses a device used by the method.
Description
Technical field
The present invention relates to take coal as raw material, perhaps take municipal wastes as raw material, perhaps take biomass fuel etc. as raw material, the mixed gas of hydrogen making and carbon monoxide, generate the technical fields such as synthetic ammonia, synthetic oil, methyl alcohol, particularly BGL vapourizing furnace or broken coal pressurization slag gasification furnace adds method and the device that non-catalytic partial oxidation is produced suitable hydrogen-carbon ratio synthetic gas or hydrogen.
Background technology
The characteristics of China's energy structure are: many coals, weak breath, oil starvation.Wherein the coal energy is at the skewness of China, and in the majority with the low grade coal of high ash content, high ash melting point, and a large amount of fat coal of power industry demand is to guarantee the high loading electricity consumption consumption in the whole nation simultaneously.So chemical industry adopts low grade coal or municipal wastes or renewable energy source to do the waste Chemicals, becomes inevitable development trend.
BGL vapourizing furnace or broken coal pressurization slag gasification furnace are to grow up on the basis of the strange fixed bed pressured gasification stove in former Shandong, the brown coal of the high ash content of the suitable gasification of this gasification technology, high-volatile, high moisture content, refinery coke, bituminous coal, municipal wastes etc., the advantages such as gasification efficiency is high, steam utilization is high, oxygen consumption is low, gasification intensity is large, thereby BGL vapourizing furnace or broken coal pressurization slag gasification furnace is compared with other vapourizing furnace, intrinsic advantage is obvious, advantages has wide market outlook.But also there are a lot of shortcomings in BGL gasification technology or broken coal pressurization slag gasification technology, and be as follows:
1. the more and complicated component of organic content in the raw gas washing gas liquor recycles difficulty, and environmental pollution is serious;
2. contain a large amount of methane in the raw gas, recycle difficulty, the long flow path investment is large; Waste raw material as not reclaiming then; Methane enters the efficient that the subsequent technique device will reduce device, and the available gas utilization ratio reduces;
3. contain organosulfur in the raw gas, such as thiophene, carbon oxysulfide, dithiocarbonic anhydride etc., also contain the components such as organism such as higher alkene, higher alkane, benzene, large on raw gas purifying technique such as low-temperature rectisol or the impact of pressure-variable adsorption workshop section.
Summary of the invention
One of technical problem to be solved by this invention is to utilize BGL stove coal generating gas to produce the existing problem of technological process of suitable hydrogen-carbon ratio synthetic gas or hydrogen and provides a kind of BGL vapourizing furnace or broken coal pressurization slag gasification furnace to add the method that the non-catalytic partial oxidation converter is produced suitable hydrogen-carbon ratio synthetic gas or hydrogen; The method is that the pure oxygen of advanced and cleaning or oxygen enrichment non-catalytic transforming technology (being called for short the POX technology) are directly combined with BGL/ broken coal pressurization slag Prospect of Gasification Technology, the problem that contains the Organic pollutants environment such as tar, light oil, phenols with thorough solution BGL vapourizing furnace or broken coal pressurization slag gasification furnace outlet raw gas, save complicated gas liquor and process workshop section, solved the difficult problem of methane content height, methane conversion flow process complexity in carbon one chemical industry.
Two of technical problem to be solved by this invention is to provide a kind of above-mentioned BGL vapourizing furnace or broken coal pressurization slag gasification furnace to add the employed device of method of non-catalytic partial oxidation converter preparing hydrogen carbon ratio synthetic gas or hydrogen.
Method as the BGL vapourizing furnace of first aspect present invention or broken coal pressurization slag gasification furnace direct-connected non-catalytic partial oxidation converter preparing hydrogen carbon ratio synthetic gas or hydrogen, it is as raw material take lump coal, pure oxygen is oxygenant, steam is vaporized chemical, fixed bed pressurization gas making, form the first raw gas of 250～500 ℃, the first raw gas directly or through dedusting enters pure oxygen non-catalytic partial oxidation converter (POX), compression pure oxygen in sending into synchronously pure oxygen non-catalytic partial oxidation converter (POX) sprays into the interior mixed firing of pure oxygen non-catalytic partial oxidation converter (POX), reach at high temperature more than 1300 ℃, make at high temperature cracking of organism, transform the second raw gas that forms more than 1300 ℃.
Described organism is organosulfur and hydrocarbons.
Described organosulfur is thiophene etc.Described hydrocarbons is methane etc.
In a preferred embodiment of the inventive method, the second raw gas that described pure oxygen non-catalytic partial oxidation converter is sent is directly delivered to the Quench washing plant that is positioned at pure oxygen non-catalytic partial oxidation converter bottom, the circulating gas water Quench washing of being brought by the gas liquor separation system, the second raw gas is washed and is cooled to 200～230 ℃, form jacket steam that the 3rd raw gas brings with described BGL vapourizing furnace or broken coal pressurization slag gasification furnace and deliver to the tube side of the useless pot of low pressure, the shell side of the useless pot of low pressure is sent in oiler feed, in the useless pot of low pressure, heat exchange is carried out in low pressure boiler feedwater in the 3rd raw gas in the tube side and jacket steam and the shell side, final formation temperature is that 140～200 ℃ the 4th raw gas is sent, and the by-product low-pressure saturated steam also is sent in the shell side; Wherein the volume ratio of the 3rd raw gas and jacket steam is 12: 1～35: 1.
In the present invention, the gas liquor that the useless pot of the washing gas liquor that described Quench washing plant forms and low pressure produces is sent the battery limit (BL) in the lump, and gas liquor forms the moisturizing of described circulating gas water or boiler systems after simple process.
In another preferred embodiment of the inventive method, the second raw gas that described pure oxygen non-catalytic partial oxidation converter is sent is directly delivered in the tube side of a thermal recovery unit, carry out heat exchange with the oiler feed of sending in the thermal recovery unit shell side, the jacket steam that the 5th raw gas is brought with described BGL vapourizing furnace or broken coal pressurization slag gasification furnace after the formation cooling is delivered to the tube side of useless pot an of low pressure, and the shell side of the useless pot of low pressure is sent in oiler feed; In the useless pot of low pressure, heat exchange is carried out in low pressure boiler feedwater in the 5th raw gas in the tube side and jacket steam and the shell side, final formation temperature is that 140～200 ℃ the 6th raw gas is sent, and wherein the volume ratio of the 3rd raw gas and jacket steam is 12: 1～35: 1; The shell side by-product middle pressure steam of wherein said heat exchanging apparatus is sent, and the useless shell journey by-product low-pressure saturated steam of low pressure also is sent.
In the present invention, the gas liquor that the useless pot of the washing gas liquor that described thermal recovery unit forms and low pressure produces is sent the battery limit (BL) in the lump, and gas liquor forms the moisturizing of described circulating gas water or boiler systems after simple process.
Described thermal recovery unit is to press useless pot in one, and its water coolant is the medium pressure boiler feedwater.
Produce the employed device of method of suitable hydrogen-carbon ratio synthetic gas or hydrogen as the BGL vapourizing furnace of second aspect present invention or the direct-connected non-catalytic partial oxidation converter of broken coal pressurization slag gasification furnace, comprise BGL vapourizing furnace or broken coal pressurization slag gasification furnace and pure oxygen non-catalytic partial oxidation converter, wherein the first raw gas outlet on BGL vapourizing furnace or the broken coal pressurization slag gasification furnace is direct-connected with the first raw gas entrance of pure oxygen non-catalytic partial oxidation converter, and the second pure oxygen spout on the described pure oxygen non-catalytic partial oxidation converter connects the pure oxygen delivery port of air separation plant by the pure oxygen input tube; On BGL vapourizing furnace or broken coal pressurization slag gasification furnace, also be provided with the first pure oxygen spout, charging opening, steam-in and slag discharge mouth; Be provided with a Quench washing plant in the bottom of pure oxygen non-catalytic partial oxidation converter, be provided with the outlet of chilled water entrance and the second raw gas on this Quench washing plant, described chilled water entrance connects the gas liquor separation system by circulating gas water transfer lime, the outlet of the second raw gas on the Quench washing plant is connected on the 3rd raw gas entrance on the useless pot of a low pressure by the second raw gas output tube, also be provided with the outlet of one the 4th raw gas on the useless pot of described low pressure, described the 3rd raw gas entrance is communicated with by the tube side in the useless pot of low pressure with the outlet of the 4th raw gas; It is 140～200 ℃ raw gas that temperature is sent in the tube side outlet of the useless pot of this low pressure; Shell side at the useless pot of described low pressure is provided with low pressure boiler admission port and low-pressure steam outlet, its middle low-pressure boiler admission port connects boiler feed water system by the useless pot feedwater of low pressure transfer lime, the outlet of the second gas liquor connects the gas liquor separation system by the second gas liquor transfer lime, and low-pressure saturated steam is sent in the low-pressure steam outlet.
Produce the employed device of method of suitable hydrogen-carbon ratio synthetic gas or hydrogen as the BGL vapourizing furnace of second aspect present invention or the direct-connected non-catalytic partial oxidation converter of broken coal pressurization slag gasification furnace, comprise BGL vapourizing furnace or broken coal pressurization slag gasification furnace and pure oxygen non-catalytic partial oxidation converter, wherein the first raw gas outlet on BGL vapourizing furnace or the broken coal pressurization slag gasification furnace is direct-connected with the first raw gas entrance of pure oxygen non-catalytic partial oxidation converter, and the second pure oxygen spout on the described pure oxygen non-catalytic partial oxidation converter connects the pure oxygen delivery port of air separation plant by the pure oxygen input tube; On BGL vapourizing furnace or broken coal pressurization slag gasification furnace, also be provided with the first pure oxygen spout, charging opening, steam-in and slag discharge mouth; On described pure oxygen non-catalytic partial oxidation converter, also be provided with the outlet of one second raw gas, described the second raw gas outlet is connected on the second raw gas entrance of a thermal recovery unit by the second raw gas output tube, on described thermal recovery unit, also be provided with the oiler feed entrance, the outlet of the first gas liquor, the outlet of the 3rd raw gas and middle pressure steam outlet, the second raw gas entrance, the interior tube side of the first gas liquor outlet and the outlet of the 3rd raw gas and thermal recovery unit is communicated with, cooling water inlet and middle pressure steam outlet are communicated with the shell side of thermal recovery unit, described oiler feed entrance connects boiler feed water system by the oiler feed transfer lime, the outlet of the first gas liquor connects the gas liquor separation system by the first gas liquor transfer lime, middle pressure steam is sent in the middle pressure steam outlet, the outlet of the 3rd raw gas is connected on the 3rd raw gas entrance of the useless pot of a low pressure by the 3rd raw gas output tube, also be provided with the outlet of one the 4th raw gas on the useless pot of described low pressure, described the 3rd raw gas entrance is communicated with by the tube side in the useless pot of low pressure with the outlet of the 4th raw gas; It is 140～200 ℃ raw gas that temperature is sent in the tube side outlet of the useless pot of this low pressure; Shell side at the useless pot of described low pressure is provided with low pressure boiler admission port and low-pressure steam outlet, its middle low-pressure boiler admission port connects boiler feed water system by the useless pot feedwater of low pressure transfer lime, the outlet of the second gas liquor connects the gas liquor separation system by the second gas liquor transfer lime, and low-pressure saturated steam is sent in the low-pressure steam outlet.
Chilled water entrance on the described Quench washing plant also is connected by the second gas liquor outlet on the useless pot of pump and water inlet branch and low pressure.
Thermal recovery unit of the present invention is the useless pot of middle pressure.
In a preferred embodiment of apparatus of the present invention, between described BGL vapourizing furnace and pure oxygen non-catalytic partial oxidation converter, can increase by a dust removal installation.
In a preferred embodiment of the invention, be provided with jacket steam outlet on described BGL vapourizing furnace or the broken coal pressurization slag gasification furnace, described jacket steam outlet is communicated with by the 3rd raw gas entrance on the useless pot of jacket steam transfer lime and described low pressure.
Owing to adopted technical scheme as above, the present invention compared with prior art has following advantage:
1.BGL the outlet raw gas of vapourizing furnace or broken coal pressurization slag gasification furnace directly enters the POX converter, and empty pure oxygen/oxygen enrichment of assigning to burns, generation high temperature transforms the organism in the raw gas fully.
2. minimally is changed former BGL gasification workshop section, guarantees the safe and stable operation of whole equipment.
3. the high-temperature gas that goes out POX adopts chilling process, and the wash cooling raw gas further reduces investment, and subsequent conversion workshop section does not need to add steam, energy-conservation energy consumption again simultaneously.
4. the raw gas after cooling is sent into the useless pot of low pressure again, further reduces the raw gas temperature, and the saturation steam that BGL vapourizing furnace chuck produces also enters the useless pot of low pressure, to guarantee not change former BGL vapourizing furnace chuck pressure balancing system.
The washing gas liquor/and the condensation gas liquor after simple process, can be used as cooling water replenishment or oiler feed moisturizing.
6. the raw gas after the present invention processes according to need of production, can by the final hydrogen of conversion adjustment/carbon monoxide ratio, satisfy the subsequent technique requirement.
7. the present invention can be used for new project, solves the problem of environmental pollution that BGL gas making brings, and also can be used for transforming former project, namely behind BGL/ broken coal pressurization slag gasification furnace, directly connects the POX converter, reaches the purpose of Increasing Production and Energy Saving.
BGL vapourizing furnace/broken coal pressurization direct-connected non-catalytic partial oxidation the converter of slag gasification furnace (POX) Prospect of Gasification Technology has the following advantages:
(1) adopts the present invention, not only can realize gasify low grade coal, domestic refuse, biomass fuel etc., and can be available gas with Substance Transformations such as the tar in the raw gas of BGL/ broken coal pressurization slag gasification furnace outlet, light oil, benzene, phenol, the acid of ester fat, make the gas liquor of whole flow process process greatly simplification.
(2) adopt the present invention, the methane content in the process gas reduces, and methane content can be down to below 0.3% from 8%～10%, and concerning producing the device that synthetic ammonia or synthesizing methanol are purpose, whole technical process is greatly simplified, and the available gas utilization ratio rises.
(3) adopt the technology of the present invention and device, if the synthetic gas that generates need to carry out transformationreation, for changing device, the conversion load reduces, the temperature of whole conversion bed is more prone to control, beds can overtemperature, more is conducive to transformation catalyst long period, steady running, saves running cost.
When (4) the present invention adopted chilling process, subsequent conversion workshop section did not need to add steam, energy-conservation energy consumption again.
(5) do not contain the impurity such as naphthalene, thiophene, light oil, tar in the raw gas, the refining plants such as rear operation low-temperature rectisol or pressure-variable adsorption are reliable stable, thereby there is not the problem of the accumulative total operation deterioration that causes impurity in the methanol solution because pollute methanol solution, do not have the problem of polluting the pressure-variable adsorption agent.
(6) adopt the present invention, the washing gas liquor is processed simple, only needs simple normal vacuum flashing to get final product Energy Intensity Reduction.This invention is compared with traditional BGL gasification gas water treatment process, and floor space reduces, and flow process shortens, and does not need the very large gas liquor separation process of floor space and complicated phenol ammonia recovery process.
Description of drawings
Fig. 1 is the skeleton diagram of apparatus of the present invention embodiment 1.
Fig. 2 is the skeleton diagram of apparatus of the present invention embodiment 2.
Embodiment
In order to make technique means of the present invention, creation characteristic, to reach purpose and effect is easy to understand, below in conjunction with specific embodiment, further set forth the present invention.
What following examples provided is a kind of to produce synthetic ammonia as the device of purpose, still is not limited to this.
Embodiment 1
Present embodiment is to produce the device that synthetic ammonia is purpose, adopts brown coal gas making, and ash content is about 30% in the coal, water-content about 15%.
Referring to Fig. 1, the employed device of method of the BGL vapourizing furnace of present embodiment or the broken coal pressurization direct-connected non-catalytic partial oxidation producing synthesis gas of slag gasification furnace or hydrogen comprises BGL vapourizing furnace 10, pure oxygen non-catalytic partial oxidation stove 20, the useless pot 40 of low pressure.
BGL stove 10 coal Gasification Technology in Retrospect adopt BGL pressurization slag gas-making process, and take brown coal as raw material, pure oxygen and steam are oxygenant/vaporized chemical, static bed gas making, slag tap.Brown coal, steam and pure oxygen are entered in the BGL stove vapourizing furnace 10 by charging opening 11, steam-in 12, the pure oxygen entrance 13 of BGL stove vapourizing furnace 10 respectively, and lime-ash is discharged by the slag-drip opening 14 of BGL stove vapourizing furnace 10.Pure oxygen is carried by pure oxygen transfer lime 51 by air separation plant 50 and is come.
About 0.69 by the ratio of hydrogen/carbon monoxide in the raw gas of BGL stove vapourizing furnace 10 outlet 15 about 400 ℃ raw gas out, and contain the methane of 7.3%V.
The raw gas condition is as follows: %V does
Other impurity are as follows:
Dust, tar, middle oil, light oil, phenol, lipid acid, ammonia, prussiate.
Adopt that hydrogen/carbon monoxide ratio is 0.58 in pure oxygen non-catalytic partial oxidation converter 20 of the present invention (POX) 1300 ℃ of high temperature rough gas out, wherein methane content is less than 0.3%V.All impurity almost all are converted into the simplest CO
2, CO, H
2And water.
Directly send into the Quench washing plant 30 that is positioned at pure oxygen non-catalytic partial oxidation converter 20 bottoms by pure oxygen non-catalytic partial oxidation converter 20 1300 ℃ of high temperature rough gas out, the Quench bath water adopts circulating gas water, sprayed into by the Quench washing water inlet 31 on the Quench washing plant 30, Quench washing water inlet 31 connects the gas liquor separation system by gas liquor transfer lime 32.Subsequent conversion workshop section does not need to add steam, energy-conservation energy consumption again like this.
After 1300 ℃ of high temperature rough gas are recycled the washing of gas liquor Quench, be cooled to about 200 ℃, send in the tube side of the useless pot 40 of low pressure by the outlet of the raw gas on the Quench washing plant 30 33, raw gas transfer lime 34.
The tube side two ends of the useless pot 40 of low pressure are respectively arranged with raw gas entrance 41, gas liquor outlet 45 and raw gas outlet 42, are respectively arranged with low-pressure steam outlet 43 and low pressure boiler admission port 44 on the shell side of the useless pot 40 of low pressure.Raw gas entrance 41 is connected with raw gas transfer lime 34 and exports 17 by the jacket steam on jacket steam transfer lime 16 and the BGL stove vapourizing furnace 10 simultaneously and is connected, the saturation steam of BGL vapourizing furnace chuck generation also enters the useless pot 40 of low pressure like this, to guarantee not change former BGL vapourizing furnace chuck pressure balancing system.
Sending into the interior raw gas of the useless pot of low pressure 40 tube sides and the volume ratio of jacket steam is 12～35, and raw gas and jacket steam enter in the tube side of the useless pot 40 of low pressure after transforming, and low pressure boiler feeds water and enters in the shell side by 44 supplies of low pressure boiler admission port.And low pressure boiler admission port 44 is connected with boiler feed water system by low pressure boiler feedwater transfer lime 46.
Heat exchange is carried out in the oiler feed interior with entering the useless pot of low pressure 40 shell sides of raw gas and jacket steam after entering the conversion in the tube side of the useless pot 40 of low pressure, and the about 180 ℃ raw gas of formation temperature exports 42 by raw gas and sends the present invention.Sent by low-pressure steam outlet 43 through the oiler feed by-product low-pressure saturated steam after the heat exchange.The gas liquor that forms send into the gas liquor separation system by gas liquor outlet 45 and gas liquor transfer lime 47 and carry out simple process, as the moisturizing of circulating gas water and boiler feed water system.
Raw gas parameter after present embodiment is processed sees Table 1:
Table 1BGL+POX raw gas
After present embodiment is processed, no longer contain the organism such as tar, light oil in raw gas/reforming gas, the coal dust that brings from gasification also major part is converted into the available gas composition, organosulfur that brings from gasification etc. also major part is converted into the inorganic sulfur that hydrogen sulfide etc. removes easily, hydrogen/carbon monoxide ratio is 0.58 in the outlet raw gas, wherein methane content＜0.3%V.
Referring to Fig. 2, the BGL vapourizing furnace of present embodiment or the direct-connected non-catalytic partial oxidation converter of broken coal pressurization slag gasification furnace are produced the employed device of method of suitable hydrogen-carbon ratio synthetic gas or hydrogen, comprise BGL vapourizing furnace 10, pure oxygen non-catalytic partial oxidation stove 20, thermal recovery unit, the useless pot 40 of low pressure.Wherein thermal recovery unit is the useless pot of middle pressure 30a.
About 0.69 by the ratio of hydrogen/carbon monoxide in the raw gas of BGL stove vapourizing furnace 10 outlet 15 about 400 ℃ raw gas out, and contain the methane of 7.3%V.
The raw gas condition is as follows: %V does
Other impurity are as follows:
Dust, tar, middle oil, light oil, phenol, lipid acid, ammonia, prussiate.
Adopt that hydrogen/carbon monoxide ratio is 0.58 in pure oxygen non-catalytic partial oxidation converter 20 of the present invention (POX) 1300 ℃ of high temperature rough gas out, wherein methane content is less than 0.3%V.All impurity almost all are converted into the simplest CO
2, CO, H
2And water.
The tube side two ends of the useless pot 40 of low pressure are respectively arranged with raw gas entrance 41, gas liquor outlet 45 and raw gas outlet 42, are respectively arranged with low-pressure steam outlet 43 and low pressure boiler admission port 44 on the shell side of the useless pot 40 of low pressure.Raw gas entrance 41 is connected with raw gas transfer lime 36a and exports 17 by the jacket steam on jacket steam transfer lime 16 and the BGL stove vapourizing furnace 10 simultaneously and is connected, the saturation steam of BGL vapourizing furnace chuck generation also enters the useless pot 40 of low pressure like this, to guarantee not change former BGL vapourizing furnace chuck pressure balancing system.
Sending into the interior raw gas of the useless pot of low pressure 40 tube sides and the volume ratio of jacket steam is 12～35, and raw gas and jacket steam enter in the tube side of the useless pot 40 of low pressure after transforming, and low pressure boiler feeds water and enters in the shell side by 44 supplies of low pressure boiler admission port.And low pressure boiler admission port 44 is connected with boiler feed water system by low pressure boiler feedwater transfer lime 46.
Heat exchange is carried out in the oiler feed interior with entering the useless pot of low pressure 40 shell sides of raw gas and jacket steam after entering the conversion in the tube side of the useless pot 40 of low pressure, and the about 180 ℃ raw gas of formation temperature exports 42 by raw gas and sends the present invention.Sent by low-pressure steam outlet 43 through the oiler feed by-product low-pressure saturated steam after the heat exchange.The gas liquor that forms send into the gas liquor separation system by gas liquor outlet 45 and gas liquor transfer lime 47 and carry out simple process, can be used as the make up water of boiler feed water system.
Raw gas parameter after present embodiment is processed sees Table 2:
Table 2BGL+POX phase coal gas
After present embodiment is processed, no longer contain the organism such as tar, light oil in raw gas/reforming gas, the coal dust that brings from gasification also major part is converted into the available gas composition, organosulfur that brings from gasification etc. also major part is converted into the inorganic sulfur that hydrogen sulfide etc. removes easily, hydrogen/carbon monoxide ratio is 0.58 in the outlet raw gas, wherein methane content＜0.3%V.
Claims (12)
1.BGL the method for vapourizing furnace or broken coal pressurization slag gasification furnace direct-connected non-catalytic partial oxidation converter preparing hydrogen carbon ratio synthetic gas or hydrogen, it is characterized in that take lump coal as raw material, pure oxygen is oxygenant, steam is vaporized chemical, fixed bed pressurization gas making, form the first raw gas of 250～500 ℃, the first raw gas directly or through dedusting enters pure oxygen non-catalytic partial oxidation converter (POX), compression pure oxygen in sending into synchronously pure oxygen non-catalytic partial oxidation converter (POX) sprays into the interior mixed firing of pure oxygen non-catalytic partial oxidation converter (POX), reach at high temperature more than 1300 ℃, make at high temperature cracking of organism, transform the second raw gas that forms more than 1300 ℃.
2. the method for claim 1, it is characterized in that, the second raw gas that described pure oxygen non-catalytic partial oxidation converter is sent is directly delivered to the Quench washing plant that is positioned at pure oxygen non-catalytic partial oxidation converter bottom, the circulating gas water Quench washing of being brought by the gas liquor separation system, the second raw gas is washed and is cooled to 200～230 ℃, form jacket steam that the 3rd raw gas brings with described BGL vapourizing furnace or broken coal pressurization slag gasification furnace and deliver to the tube side of the useless pot of low pressure, the shell side of the useless pot of low pressure is sent in oiler feed, in the useless pot of low pressure, heat exchange is carried out in low pressure boiler feedwater in the 3rd raw gas in the tube side and jacket steam and the shell side, final formation temperature is that 140～200 ℃ the 4th raw gas is sent, and the by-product low-pressure saturated steam also is sent in the shell side; Wherein the volume ratio of the 3rd raw gas and jacket steam is 12: 1～35: 1.
3. the method for claim 1, it is characterized in that, the gas liquor that the useless pot of the washing gas liquor that described Quench washing plant forms and low pressure produces is sent the battery limit (BL) in the lump, and gas liquor forms the moisturizing of described circulating gas water or low pressure boiler water feeding system after simple process.
4. the method for claim 1, it is characterized in that, the second raw gas that described pure oxygen non-catalytic partial oxidation converter is sent is directly delivered in the tube side of a thermal recovery unit, carry out heat exchange with the water coolant of sending in the thermal recovery unit shell side, form the 5th raw gas is brought with described BGL vapourizing furnace or broken coal pressurization slag gasification furnace after the cooling jacket steam and deliver to the shell side that the useless pot of low pressure is sent in the tube side oiler feed of the useless pot of a low pressure; In the useless pot of low pressure, heat exchange is carried out in low pressure boiler feedwater in the 5th raw gas in the tube side and jacket steam and the shell side, final formation temperature is that 140～200 ℃ the 6th raw gas is sent, and wherein the volume ratio of the 3rd raw gas and jacket steam is 12: 1～35: 1; The shell side by-product middle pressure steam of wherein said heat exchanging apparatus is sent, and the useless shell journey by-product low-pressure saturated steam of low pressure also is sent.
5. method as claimed in claim 4 is characterized in that, the gas liquor that the useless pot of the washing gas liquor that described thermal recovery unit forms and low pressure produces is sent the battery limit (BL) in the lump, and gas liquor forms described boiler feed water system moisturizing after simple process.
6. method as claimed in claim 5 is characterized in that, described thermal recovery unit is to press useless pot in one, and its water coolant is the medium pressure boiler feedwater.
7. the direct-connected non-catalytic partial oxidation converter of BGL vapourizing furnace as claimed in claim 2 or broken coal pressurization slag gasification furnace is produced the employed device of method of suitable hydrogen-carbon ratio synthetic gas or hydrogen, comprise BGL vapourizing furnace or broken coal pressurization slag gasification furnace and pure oxygen non-catalytic partial oxidation converter, wherein the first raw gas outlet on BGL vapourizing furnace or the broken coal pressurization slag gasification furnace is direct-connected with the first raw gas entrance of pure oxygen non-catalytic partial oxidation converter, and the second pure oxygen spout on the described pure oxygen non-catalytic partial oxidation converter connects the pure oxygen delivery port of air separation plant by the pure oxygen input tube; On BGL vapourizing furnace or broken coal pressurization slag gasification furnace, also be provided with the first pure oxygen spout, charging opening, steam-in and slag discharge mouth; Be provided with a Quench washing plant in the bottom of pure oxygen non-catalytic partial oxidation converter, be provided with the outlet of chilled water entrance and the second raw gas on this Quench washing plant, described chilled water entrance connects the gas liquor separation system by circulating gas water transfer lime, the outlet of the second raw gas on the Quench washing plant is connected on the 3rd raw gas entrance on the useless pot of a low pressure by the second raw gas output tube, also be provided with the outlet of one the 4th raw gas on the useless pot of described low pressure, described the 3rd raw gas entrance is communicated with by the tube side in the useless pot of low pressure with the outlet of the 4th raw gas; It is 140～200 ℃ raw gas that temperature is sent in the tube side outlet of the useless pot of this low pressure; Shell side at the useless pot of described low pressure is provided with low pressure boiler admission port and low-pressure steam outlet, its middle low-pressure boiler admission port connects boiler feed water system by the useless pot feedwater of low pressure transfer lime, the outlet of the second gas liquor connects the gas liquor separation system by the second gas liquor transfer lime, and low-pressure saturated steam is sent in the low-pressure steam outlet.
8. device as claimed in claim 7 is characterized in that, the chilled water entrance on the described Quench washing plant also is connected by the second gas liquor outlet on the useless pot of pump and water inlet branch and low pressure.
9. BGL vapourizing furnace or the direct-connected non-catalytic partial oxidation converter of the broken coal pressurization slag gasification furnace employed device of method of producing suitable hydrogen-carbon ratio synthetic gas or hydrogen as second aspect present invention as claimed in claim 4, comprise BGL vapourizing furnace or broken coal pressurization slag gasification furnace and pure oxygen non-catalytic partial oxidation converter, wherein the first raw gas outlet on BGL vapourizing furnace or the broken coal pressurization slag gasification furnace is direct-connected with the first raw gas entrance of pure oxygen non-catalytic partial oxidation converter, and the second pure oxygen spout on the described pure oxygen non-catalytic partial oxidation converter connects the pure oxygen delivery port of air separation plant by the pure oxygen input tube; On BGL vapourizing furnace or broken coal pressurization slag gasification furnace, also be provided with the first pure oxygen spout, charging opening, steam-in and slag discharge mouth; On described pure oxygen non-catalytic partial oxidation converter, also be provided with the outlet of one second raw gas, described the second raw gas outlet is connected on the second raw gas entrance of a thermal recovery unit by the second raw gas output tube, on described thermal recovery unit, also be provided with the oiler feed entrance, the outlet of the first gas liquor, the outlet of the 3rd raw gas and middle pressure steam outlet, the second raw gas entrance, the interior tube side of the first gas liquor outlet and the outlet of the 3rd raw gas and thermal recovery unit is communicated with, oiler feed entrance and middle pressure steam outlet are communicated with the shell side of thermal recovery unit, described oiler feed entrance connects boiler feed water system by the oiler feed transfer lime, the outlet of the first gas liquor connects the gas liquor separation system by the first gas liquor transfer lime, middle pressure steam is sent in the middle pressure steam outlet, the outlet of the 3rd raw gas is connected on the 3rd raw gas entrance of the useless pot of a low pressure by the 3rd raw gas output tube, also be provided with the outlet of one the 4th raw gas on the useless pot of described low pressure, described the 3rd raw gas entrance is communicated with by the tube side in the useless pot of low pressure with the outlet of the 4th raw gas; It is 140～200 ℃ raw gas that temperature is sent in the tube side outlet of the useless pot of this low pressure; Shell side at the useless pot of described low pressure is provided with low pressure boiler admission port and low-pressure steam outlet, its middle low-pressure boiler admission port connects boiler feed water system by the useless pot feedwater of low pressure transfer lime, the outlet of the second gas liquor connects the gas liquor separation system by the second gas liquor transfer lime, and low-pressure saturated steam is sent in the low-pressure steam outlet.
10. device as claimed in claim 9 is characterized in that, described thermal recovery unit is the useless pot of middle pressure.
11. such as claim 7 or 9 described devices, it is characterized in that, between described BGL vapourizing furnace and pure oxygen non-catalytic partial oxidation converter, increase by a dust removal installation.
12. such as claim 7 or 9 described devices, it is characterized in that, be provided with jacket steam outlet on described BGL vapourizing furnace or the broken coal pressurization slag gasification furnace, described jacket steam outlet is communicated with by the 3rd raw gas entrance on the useless pot of jacket steam transfer lime and described low pressure.
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| CN2011102957998A CN103031154A (en) | 2011-09-30 | 2011-09-30 | Method and device for preparing synthesis gas or hydrogen by direct connection of non-catalytic partial oxidation furnace with BGL gasifier or crushed coal pressurized slag gasifier |
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| CN2011102957998A CN103031154A (en) | 2011-09-30 | 2011-09-30 | Method and device for preparing synthesis gas or hydrogen by direct connection of non-catalytic partial oxidation furnace with BGL gasifier or crushed coal pressurized slag gasifier |
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Application publication date: 20130410 |