DE3217422A1 - Process and equipment for processing comminuted coal by gasification by means of a multi-chamber reactor - Google Patents

Abstract

The process and the equipment according to the invention have the purpose of obtaining very largely phenol- and tar-free gas with a calorific value, which is not achievable according to the state of the art, of, for example, 1120-1150 kcal in a pyrolysis chamber. As Figure 1 shows, a multi-chamber reactor is used for this purpose, in the centre of which cyclone is incorporated, around which, in the interior, a combustion chamber and, on the adjacent exterior, a pyrolysis chamber are arranged. A cracking chamber surrounded by an annular flue gas chamber is provided downstream of the upper cyclone outlet. At a degree of coal conversion of 99%, a gasification efficiency of 70 to 75% is reached, the CO2 content not exceeding the norm and ignitions being reliably prevented due to the flow of inert flue gas through the coal grit and/or dust.

Description

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The invention relates to "a method for processing coal by Gasification by means of a multi-chamber reactor, with the aim of a largely phenol and tar-free gas with increased railroad tracks Calorific value, with a high gasification efficiency of the gas generated in a pyrolysis chamber, as well as a device for implementation of the procedure.

The known techniques of fluidized bed generator systems have a common disadvantage, that of the high carbon loss consists. This loss occurs when the carbon is discharged from the fluidized bed usually used, together with the escaping gas, in the form of dust and also in the form of teüvergaslen particles.

Numerous attempts have been made to reduce this loss- Contain the process through different, constructive solutions. Most of these solutions are mechanical Return devices, which involve a very considerable amount of effort

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bring yourself and also have the disadvantage of the heat; -au ;. stop of the generator unfavorably ^ u. Don't go wrong with these solutions is the other one ^! .: Leading the ashes into the procedural process

The invention has set itself the task of bi. NEN disadvantages 2u avoid and yet a near ..u 1O * ", to ensure gassing of the introduced carbon, whereby the construction can be designed in such a way that a higher value The cracking of the heavy hydrocarbons or the water introduced is not possible.

The invention solves this problem by starting from a method according to the preamble of claim 1 ", and they is characterized by the fact that the pyrolysis gas flowing out is largely cleaned of solid components in a cyclone, then a fluidized bed combustion chamber, g also while adding oxygen, happens and the through do Flue gas preheated combustion chamber as synthesis gas / cr; äi3 ».

Figures 1 to 4 show exemplary embodiments ⁵ ": r! .Zrfindung. Fcs show:

ORIGINAL INSPECTED

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Fritz Werner: "Procedure"

Figure 1 is a sectional view of the reactor with egg

ner crack chamber in the upper part, a cyclone in the center of the middle part and the feed and discharge devices in the lower part,

Figure 2 shows a reactor in the center of a Zy

is arranged clone and an inflow plate with tangentially arranged nozzles, as well Locks for the discharge of the lock chambers and

Figure 3 is a process scheme with the fiction

appropriate multi-chamber reactor in the core of the overall system.

FIG. 1 shows the typical form of the arrangement according to the invention a cyclone 20 in the core of the multi-chamber reactor. This cyclone 20 has the task of the non-gasified solid carbon particles from to separate the outflowing gas and convey it through the underflow of the cyclone 20 into the fluidized bed combustion chamber 21.

In this fluidized bed combustion chamber, water vapor takes place - Air - mixture or by means of purging gas the afterburning. If necessary, by means of the arranged in the core of the reactor

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The fluidized bed and additional cracking can be prevented.

For this remnant carbon-forking are ideally suitable. Lignite. * - :, anthracite undiBraunkohlenkoks in Grieeforrcr »^ et ™ RegelPait v a margin of 0.5 to 5 mm and make up the" ws-ärnrnen with 'a Wa serdampf-LuftHSemtschi or oxygen mixture erft ^ dung-sgett ■ ·.,;. to be gassed. These types of coal are added to the pyrolysis chamber 22 by means of the feed screw 26.

The gas flowing out of the fluidized bed of the pyrolysis chamber 22 is due to the double deflection in the area of the pyotysis chamber 22 and of the cyclone 20 freed from the larger carbon particles and in the fluidized bed combustion chamber 21 wnd the fluidized oil there returned.

In the lower part of the reactor there is a k * g # Uge · * ÄJiströmbodc.n 12. The ash residue melted into slag flows over the lower exit of the conical oil tube 12 to the slag slide 53 according to FIG. 2 from *

In a special embodiment of the invention that is used for generating of pure synthesis gas is used instead of the inner fluidized bed a fluidized bed combustion chamber 21 is used in the core of the reactor 10, as FIG. 2 shows. In this brewing chamber, some of the gas and the outside of the outer bed 22 are also discharged solid carbon particles.

. ORIGINAL INSPECTED

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Fritz Werner: "Procedure"

The i> o erzeugfu heat is supplied to the outer pyrolysis layer in the pyrolysis chamber 22nd The gasification and turbulence also takes place in this layer using flushing gas and HO steam. That steam

ο is set to 500 C in a heat exchanger connected downstream of the reactor heated. The combustion air must then have approximately the same temperature.

The previously described process and its facility for processing of coal is an allothermic process in which the energy for gasification by burning the residual carbon with hot air is carried out in the fluidized bed combustion chamber 21.

The degassing and gasification takes place with exclusion of air in the outside Fluidized bed chamber 22. The structural arrangement of the annular chambers 21 and 22 allows a very intensive heat transfer the fluidized bed chambers with each other. This results in a low heat loss, which is caused by a kind of immersion boiler effect in the combustion chamber 21 is still enlarged.

The complete cracking of the higher hydrocarbons takes place in the upper part of the combustion chamber shaft, within the flue gas ring flowing out of the fluidized bed, at a temperature of around 1100 ° C the downstream cracking chamber 30, instead of, in this cracking chamber there is the fluidized bed 31, which is located above the inflow tray 32

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Fritz Werner: "Procedure."

is ordered. The fluidized bed in the cracking chamber 30 consists - suu ii .. tem, highly heat-resistant material with a grain size of about 1 mm. . ■> to bind the released carbon is directly above the .- · - ■ s ;, the oxygen by means of the entry line 35 and a:> ü?, O eu. The hot gas now generated leaves the reactor with approx.: -Nl · hot gas has a negligible accumulation part of approx. mg / Nn. The ash is discharged through the open, conical inflow base 12 in liquid form as slag. The _Hp O steam and gas discharge 13 opens tangentially via the supply line 14 into the nozzles 23, and the air is sent via the supply line t4 to the openings of the conical inflow base 12, or under ⁴ the pyrolysis grate 27 printed.

Through the process, the residual carbon released from the gas Burning with the use of an optimal heat balance is at the same time a high one with a coal conversion rate of 99% Gasification efficiency (with synthesis gas generation) of 70 - ^ 5% moy borrowed. In order to achieve this high level of efficiency, the heat is gie of the flue gas and the raw gas are almost completely used to reduce the or combustion agent and the gasification ^. ·; 'off to preheat or to heat. This takes place in 2 separate currents:.! On "firi.

On the flue gas side of the H _o is 0 heated steam for the gasification at 600 C in a waste heat boiler etwn A3. With the flue gas pre-cleaned in a cyclone tiO, which is raised in the waste heat boiler from 1000 to approximately 400 C

../U) . . . ORIGINAL INSPECTED

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is cooled down ", the coal is ground to a grain size of 1 - 4 mm pneumatically from the mill 42 into the preheating and dosing bunker

transported and preheated here by the flue gas to approx. 250 C in direct current. Dns flue gas leaves the bunker above the lower sluice and flows through the raw coal bunker 41 to dry and heat the coal to 100 C, in order to be released into the environment via a chimney. The CO share does not exceed the limits of the usual lean gas generators. The flow of coal or dust with the internal flue gas prevents ignition.

Some of the gas can after cleaning with a temperature from about 250 ° C. to the reactor 10 again as purge gas will.

In the waste heat boiler 46, the combustion air is heated to around 600.degree. . By preheating the Vcrgn-sungsmi ttel and, incombustible material intensive gasification with very rapidly occurring reaction is to just above the distributor plate be made possible to the aforementioned high V <ryn;?, Uncjswirkunn ^c; to achieve grnd.

To reduce the sulfur content in the exhaust ·; will be over you · mill 42 pt about 5% lime added, which is part of the sulfur in the A: -che

.'ur OnSO "binds.
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List of reference numbers

Do multi-chamber reactor

11 reactor lock

12 conical inflow plates

13 Steam and purge gas inlet

14 Hot air supply line

20 cyclone

21 fluidized bed combustion chamber

22 pyrolysis chamber

23 nozzles in 21 (tangential)

24 cyclone outlet, top

25 cyclone outlet, below

26 entry in 22 (snail)

27 Rotatable pyrolysis grate (inflow tray)

28 Supply line for purge gas

29 Combustion chamber outlet opening

30 crack chamber

31 fluidized bed in 30

32 Manifold

33 Flue gas annular chamber

34 Flue gas outlet

35 Oxygen entry line

40 Rohkohieburuer .- :; , <t

41 raw coal horn. tion

42 mill with classifier

43. Lime bunker with Dost-l · .-

44 preheating υ. Dosi erb

45 Dosing sluice

46 Waste heat boiler (Heiei -! .- generation)

47 'Hei ßgasftlter

4Ö. Niederfompf! Ra1ur-K 50 ', R auc hg aa -Z yk I on 5t waste heat boiler (H ₀ O-

generation) • 52 Rau c hg asf i I te r

53 slag sluice

54 Rauch-Wälzgas-Geb

55 purge gas blower

56 Ash disposal

ORIGINAL INSPECTED

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Claims (8)

A. Mal Hit: Fritz Werner Industrial Equipment GmbH, 6222 Gtn "Procedure and equipment for processing zet small by gasifying using a multi-chamber reactor" Patent to Sprüche 1.y Process for the preparation of reduced coal by gasification by means of a multi-chamber reactor in order to obtain a gas as far as possible free of phenol and tar with a comparatively increased calorific value and high gasification efficiency. Received 'means gas generated in a pyrolysis chamber, characterized in that the pyrolysis gas Ir, -Λ-nem cyclone (20) largely cleaned of solid constituents, then an inflow tray (32) with a fluidized bed (31) above it with the addition of oxygen is cracked hydrogenating and the cracking chamber (30), which has been preheated by F ^ also gas, leaves as pure gas. (Fig. 1) ../2 ORIGINAL INSPECTED / um · - ιικι in ν of May 4, 1982; />; cat, D ^ ts «means godfather camouflages μίλι ι Fritz Werner: "Procedure" 2. The method according to claim 1, characterized in that that adding the for the cracking temperature of about 950 C required amount of heat, allothermal (from outside to inside) takes place. 3. The method according to claims 1 and 2, characterized in that the allothermal heat through the Gas flow of the upper cyclone outlet (24) is increased. (Fig. 1) 4. Device for processing crushed coal in a multi-chamber fluidized bed reactor according to the claims 1 to 3 by gasifying and producing a phenol- and tar-free gas with a comparatively higher calorific value, with high carburetor efficiency, the chambers of which have fluidized beds that are heated by hot air, purge gas or Purge gas-vapor mixture are flowed through, thereby characterized in that in the core of the reactor a cyclone (20) and around it, directed from the inside to the outside, a combustion chamber (21) and a pyrolysis chamber (22) are arranged. (Fig. 1 and 2) from May 4, 1982 V.ön. .the. "(^ uteLhe'Rät & ulinl J. Fritz Werner: "Procedure ..." 5. Device according to claim 4, characterized by gekoiini-eichiu that the upper Zykon outlet (24) is one of a flue gas ring chamber (33) Surrounded crack chamber (3O) night / u;. <.- h. ■: ■ is, which is a fluidized bed (31) made of ÄtüHiiniurnö'xydyr. «··. -above of a supply base (32). (Fig. 1) 6. Device according to claims 4 and 5, characterized in that that in the lower part I of the combustion chamber (21) a funnel-shaped, downwardly open outflow opening (29) is arranged with an adjoining lock (11) (Fig. 1) 7. Device according to claims 4 to 6, characterized in that The lower cyclone outlet (25) in the predominant part of the combustion chamber (21) and the Fluidized bed immersed. (Fig. 1) 8. Device according to claims 4 to 7, characterized in that that the grate (27) is designed as a rotating grate. (Fig. 1) •• / 4 ORIGINAL INSPECTED