JPS61185591A - Manufacture of gas - Google Patents

Abstract

(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.

Description

DETAILED DESCRIPTION OF THE INVENTION [Industrial Application] The present invention relates to the production of carbonaceous materials from carbonaceous materials, including the vaporization and partial combustion of fine carbonaceous materials and subsequent heating of the product gas mixture in a coke-filled oven. The present invention relates to a method for producing gases containing mainly CO and H2, as well as an apparatus for carrying out this method.

[Conventional technology]

There are several different methods known in the prior art for the production of reducing gases and synthesis gases of the type referred to herein, and the internal proportions of CO and H2 in the gases obtained by these various methods are Generally different. Furthermore, these known methods are limited in that the content of CO□ and H2O in the generated gas is low.

It is also known that the gas produced can be heated by passing it through an oven filled with coke. However, a disadvantage of this known process is that this coke accounts for approximately 10% of the total consumption of carbon carrier.
It is to become q6.

Reactive coke is required to effectuate arblation at the desired low temperatures.

Thermal, it is known to produce reactive coke at low temperatures, and this is done in connection with the extraction of tar. Significant benefits are obtained from the use of reactive coke compared to commercially available coke. It is smokeless and odorless when burned and can be ignited at low temperatures, ie at about 600°C.

Limited availability of reactive coke forces the use of commercial metallurgical coke today;
It is less reactive and therefore requires higher temperatures for heating up. This results in the exothermic reaction ending before the desired amounts of CO and H2 are obtained.

[Purpose of the invention]

The object of the present invention is a process for the production of a gas containing primarily CO and H2, independent of its volatile composition, from any carbonaceous starting material, thereby eliminating the volatile fraction present in the initial carbonaceous material. can be used and also CO and H
The aim is to obtain a production method in which the physical heat derived from the volatile part and part of the coke can be recovered in the process.

Another object of the invention is to produce a reactive coke for use in the process described above for complete heating of the gas produced in the process.

Yet another object of the invention is to obtain an apparatus for carrying out the method of the invention.

[Description of Means and Examples for Accomplishing the Objects] The object is to carbonize a lumpy carbonaceous starting material in a furnace while supplying external energy and an oxidant; According to the consumption of coke in the intensifier furnace to heat up the gas mixture obtained after vaporization and partial combustion, a gas-tight system is installed.
the hot gas obtained from carbonization and containing the volatile part of the carbonaceous starting material is used for the decomposition and reformation of the components contained therein and for the reduction of its physical calorific value. This is achieved by the present invention, which is primarily characterized by its introduction into a vaporization process for utilization.

Preferably, CO□ and H2O in the produced product gas
The content of CO and H is adjusted from 0 to 10%, thereby reducing CO and H
The content of 2 is 100 to 90%.

According to one embodiment of the invention, the carbonization of the initial carbonaceous material is carried out at a temperature of 600-800<0>C.

A highly reactive coke is thereby obtained, which is fed directly into the connected intensifier through a gas-tight, coke system, so that it is never exposed to, for example, atmospheric oxygen.

According to another embodiment of the invention, the mass of carbonaceous material is anthracite;
Consisting of asphaltic coal, lignite and/or peat.

According to yet another embodiment of the invention, the production in the carbonization furnace is performed using a level sonde in the intensifier furnace.
adjusted by. The raw material used can be any carbonaceous material, e.g. peat, but e.g.
In order to obtain a gas consisting of 0.00% CO and H2, although reactive coke is used, the coke can be consumed to a higher extent in the intensifier if necessary.

The carbonaceous starting material is partially oxidized and carbonized while simultaneously applying external energy and oxidant in a carbonization furnace.

According to another embodiment of the invention, the oxidant is 02, H2O
and/or added in the form of a gas containing CO2. This allows the oxidant to be completely or partially preheated before it is introduced into the carbonization furnace, and the discharged hot product gases can be utilized for this purpose.

According to yet another embodiment of the invention, before the oxidant is introduced into the carbonization furnace, it is fed in whole or in part through a combustion chamber containing an oil- or gas-fired burner. When igniting the gas in the burner, a cooled and compressed product gas is used, which gas may be heat exchanged with the hot product gas before being fed to the burner.

According to yet another embodiment of the invention, the coke produced in the carbonization furnace is cooled before being discharged from the carbonization furnace. This is done by introducing cooled and compressed product gas into the discharge chamber of the carbonization furnace. Alternatively, cooling can be achieved by cooling the discharge table.

This makes the coke easier to handle in the hermetic passageway, and also makes the choice of material for the passageway system less critical.

The invention also includes an apparatus for carrying out the method of the invention as described above, which apparatus consists of a gas production section with a vaporization chamber and an intensifier, and a gas-tight supply unit for the carbon carrier mass, and A carbonization furnace connected to an intensifier through an airtight feed unit for the carrier mass. It is mainly characterized by a supply unit for oxidant and energy, a discharge unit at the bottom of the carbonization furnace for the reactive coke produced, and an upper outlet for the coke oven gas produced in carbonization.

According to one embodiment of the inventive device, the inventive device includes a cooling gas supply unit arranged to open into the discharge chamber (which also includes the discharge device) of the carbonization furnace.

According to another embodiment of the invention, the apparatus of the invention comprises a gas conduit from the gas outlet of the carbonization furnace to the vaporization chamber, whereby the volatile portion of the bulk carbonaceous starting material is transferred to the vaporization chamber for decomposition and reforming. supplied directly into the

According to a further embodiment of the apparatus according to the invention, the apparatus according to the invention comprises a conduit and a heat exchange means for heat exchange with the heat product gas, comprising compressor means for supplying the oxidant to the carbonization furnace. including.

According to a further embodiment of the device according to the invention, the device according to the invention includes a combustion chamber in the conduit for the supply of oxidant.

According to a further embodiment of the device of the invention, an oil or gas combustion nozzle is arranged in the combustion chamber.

According to a further embodiment of the inventive device, the inventive device comprises a conduit for the circulation of the product gas, which includes a cooling unit and a subsequent compressor, and which conduit opens into the burner. ing. This recirculation conduit preferably includes a pinous unit so that the product gas is freely, wholly or partially heat exchanged.
It may further include a heat exchanger for exchanging heat between the cooled and compressed product gas and the hot product gas.

The invention will be described in more detail below with reference to the drawings, which show a preferred embodiment of a plant for carrying out the method of the invention.

The gas production part of the apparatus includes a vaporization unit with a chamber 1 for vaporization and partial combustion of finely divided carbonaceous starting material and an intensifier 2 filled with coke 3.

The vaporization chamber is preferably designed as a cylindrical chamber with walls 4,5. There can be several vaporization chambers connected to the intensifier. One or several slab outlets 6 are arranged for the discharge of slabs from the intensifier and the vaporization chamber. The produced gas is taken out through a gas outlet lower in the upper part of the intensifying furnace.

The carbon carrier mass is fed to the intensifier through a gas-tight lock system 8 opening into the top of the intensifier. Vaporization chamber 1
is open into the lower part of the intensifier, and gas passes from the vaporizing chamber upwardly through the coke bed and exits through a gas outlet.

At least one /? - A gas generator is installed in the vaporization chamber, which in the illustrated embodiment consists of a plasma generator 9. The plasma generator is attached to the vaporization chamber via a valve mechanism 10. The oxidant is introduced into the plasma generator by supply conduit 11. The oxidant can be used as a carrier gas, which can be directed through a plasma generator, or alternatively a separate carrier gas can be used. The hot turbulent gas produced in the plasma generator is directed into the vaporization chamber through the plasma generator mouth 12. Carbonaceous fuel, preferably carbonaceous material in powdered form, is added through a supply conduit 13 into a concentric ring column 14 disposed around the mouth of the plasma generator and/or through a lance 15, which includes any necessary It can also be used for the supply of additives.

In the intensifier furnace, lances 16, 17 are arranged for the utilization of the excess physical heat in the gas and for the supply of further optional oxidants, such as, for example, H2O, Co□.

This therefore also allows adjustment of the temperature and composition of the gas.

For temperature measurement and/or gas analysis, a first sensing device 18 is arranged in the vaporization chamber near the point of coke addition, and a second sensing device 18 is placed in the gas exit lower from the intensifier. A device 19 is arranged and with the help of these two sensing devices the process can be controlled.

A lance 20 is arranged in the vaporization chamber 1 for supplying slab-forming components.

The device has a supply unit for bulk carbonaceous starting material 23)2
It also includes a carbonization furnace 21 having 2 carbonization furnaces. The oxidant and external energy are supplied through a parallel tube 2 with a tuyere 25 opening into the carbonization furnace.
Supplied through 4.

At the bottom of the carbonization furnace, a discharge unit is arranged in the form of a rotary table 26 with a conduit 27, which is directly connected to the airtight locking system 8 for introducing the lump coke into the intensifier. There is.

The oxidant in the form of a gas containing O2, H2O and/or C02 passes through conduit 28 and compressor 29 and into parallel tube 2.
4 and tuyere 25 to the carbonization furnace. Thereby, the oxidant can be preheated in whole or in part in the heat exchanger 30 using a hot product bus passing through a conduit 31 that is directly connected to the product gas outlet 32.

External energy can be provided by burning oil or gas.

If oil is used, the oil is combusted in a burner 33 opening into the combustion chamber 34, whereby the oxidant is fed wholly or partially through the combustion chamber via conduit 35. Thereby, the oxidant can be completely or partially preheated in the heat exchanger 30.

If gas is used for the supply of external energy, a portion of the produced product gas is withdrawn through conduit 36 and cooled in a cooling unit 37, after which the cooled gas is transferred to a compressor 38.
Compress it to the required pressure inside. Therefore, the gas can be preheated wholly or partially in a heat exchanger 39 in which the cold product gas is heat exchanged with the hot exhaust product gas supplied through the conduit 40. do.

The product gas thus cooled, compressed and, if necessary, preheated, is then introduced through the combustion chamber 33 into the combustion chamber 34 .

The coke produced in the carbonization furnace may be cooled prior to removal from the furnace to facilitate handling in the gas-tight channels. This can be done according to one embodiment of the invention by feeding a partial stream of the cooled and compressed product gas from the compressor 38 through a branch conduit 42 into the discharge chamber 41 of the carbonization furnace.

The coke oven gas produced by carbonization is fed from an outlet 43 at the top of the carbonization oven through a conduit 44 to the vaporization chamber IK. The gas thereby exhibits a temperature of 500-700°C and contains volatile parts of the carbonaceous starting material. In this method, the energy is utilized at the same time that the components of the gas can be decomposed and reformed directly in the vaporization chamber.

Therefore, according to the present invention, the reactive coke for heating is
By-products during the production of reactive coke are simultaneously converted into valuable gases and are obtained in the required quantities.

Typically, the fine carbon carrier added to the vaporization chamber makes up about 85% of the product gas produced, the recycled coke oven gas makes up about 5%, and the reactive coke in the heating furnace makes up about 5%. It makes up about 10%.

Additionally, the product gas typically contains about 20 inches of H2 and CO.
804, but this proportion can be varied, for example, by utilizing water vapor as the oxidant in the combustion chamber.

[Brief explanation of the drawing]

The drawing shows a preferred embodiment of a plant for carrying out the method of the invention. In the figure, 1 is a vaporization chamber, 2 is a heating furnace, 3 is coke, 6 is a slag outlet, 7 is a gas outlet, 8 is an airtight lock system, 9
is a plasma generator, 10 is a valve mechanism, 11.13 is a supply conduit, 14 is a concentric ring column, 15.16.17.20
is a lance, 18.19 is a detection device, 21 is a carbonization furnace, 22
2 is a supply unit, 23 is a carbonaceous starting material, 24 is a parasol tube, 25 is a tuyere, 26 is a rotary table, 27 is a conduit, 2
9 compressors, 30 heat exchangers, 33 nono-na, 34
is a combustion chamber, 37 is a cooling unit, 38 is a compressor, and 39 is a heat exchanger.

Claims (1)

Claims: 1. Predominantly CO and H_ from a carbonaceous starting material, including a step of vaporization and partial combustion of the finely divided carbonaceous starting material and a subsequent heating step of the product gas mixture in a coke-filled oven.
2. A process for producing gas consisting of carbonizing a bulk carbonaceous starting material in a furnace while supplying external energy and an oxidant, and passing the reactive coke produced in the carbonization furnace through an airtight locking system for vaporization and partial To increase the heat of the gas mixture obtained after combustion, the coke is added into the intensifier depending on the consumption of coke in the intensifier, which is also produced by carbonization, and the volatile part of the carbonaceous starting material 1. A gas production method characterized by introducing a hot gas containing . 2. Adjust the amount of CO_2 and H_2O in the produced product gas to 0 to 10%, and reduce the content of CO and H_2 to 10%.
2. The method according to claim 1, characterized in that the adjustment is made between 0 and 90%. 3. Process according to claim 1, characterized in that the carbonization of the carbonaceous starting material is carried out at a temperature of 600 to 800C. 4. characterized in that the carbonaceous starting material consists of lumps of anthracite, asphalt-containing coal, lignite and/or peat briquettes;
A method according to claim 1. 5. The method according to claim 1, characterized in that the carbonization step is controlled by a level sonde in a heating furnace. 6. Process according to claim 1, characterized in that a gaseous oxidant consisting of O_2, H_2O and/or CO_2 is added to the carbonization furnace. 7. Process according to claim 6, characterized in that the oxidant is preheated in whole or in part by heat exchange with a hot product gas. 8. The method according to claim 6 or 7, characterized in that the oxidant, before being introduced into the carbonization furnace, is conducted wholly or partially through a combustion chamber containing an oil or gas-fired burner. Method. 9. Claim 8, characterized in that the cooled and compressed product gas is used as the burner gas.
The method described in section. 10. Process according to claim 9, characterized in that the cooled and compressed product gas is heat exchanged with hot product gas before entering the burner. 11. The method according to claim 1, characterized in that the coke produced in the carbonization furnace is cooled before being removed from the furnace. 12. Process according to claim 11, characterized in that a cooled and compressed partial stream of the gas produced in the intensifier is used for cooling the coke. 13. The method according to claim 11, characterized in that the coke is cooled by water cooling in a coke discharge unit. 14. Vaporization and partial combustion of the fine carbonaceous starting material and subsequent enrichment of the product gas mixture in a coke-filled oven, including a gas production section with a vaporization chamber and a heating furnace and a gas-tight feed unit for the carbon carrier mass. In an apparatus for thermally producing gases containing mainly CO and H_2 from carbonaceous starting materials, a carbonization furnace ( 21), a supply unit (24, 25) for oxidant and energy, a discharge unit (26) at the bottom of the carbonization furnace for the reactive coke produced and an upper part for the coke oven gas produced by carbonization. Exit (43
). 15. The cooling gas conduit (42) is connected to the discharge unit (26)
15. Device according to claim 14, characterized in that it is arranged to open into a discharge chamber (41) of a carbonization furnace containing a carbonization furnace. 16. Claim 14, characterized by a gas conduit (44) from the gas outlet (43) of the carbonization furnace to the vaporization chamber (1)
Apparatus described in section. 17. Compressor means (
29), characterized by conduits (28, 35) and heat exchange means (30) for heat exchange with the thermal product gas;
An apparatus according to claim 14. 18. Device according to claim 17, characterized by a combustion chamber (34) placed in a conduit (35) for the supply of oxidant. 19. Device according to claim 17, characterized by an oil- or gas-fired burner (33) arranged in the combustion chamber (34). 20. Cooling unit (3) for circulating product gas
19. Device according to claim 18, characterized by a conduit (36) comprising a compressor (38) following it and a compressor (38) and opening into the burner (33). 21, Patent, characterized in that the circulation conduit (36) comprises a heat exchanger (39) for heat exchange with the hot product gas as well as a bypass conduit (36a) passing through the heat exchanger (39) Apparatus according to claim 20.