DE102006022265A1 - Synthesis gas`s ingredient gasification method, involves holding fluidized bed in controlled movement by driving nozzle that feeds water vapor and/or synthesis gas in reactor such that reaction zone is enlarged - Google Patents

Abstract

The method involves providing a gasifier, which has an impulse burner, with a fluidized bed in the gasifier. The fluidized bed is held in a controlled movement by a driving nozzle that feeds water vapor and/or synthesis gas in a reactor in such a manner that a reaction zone is enlarged. The driving nozzle is arranged underneath the fluidized bed, where the movement of the fluidized bed is controlled and regulated by jet nozzles. The enlargement of the reaction zone is achieved for flash pyrolysis. An independent claim is also included for a device for gasification of ingredient in synthesis gas.

Description

Field of the invention:

The Development of thermal gasification processes has essentially produced three different carburetor types, the entrained flow gasifier, the fixed bed gasifier and the fluidized bed gasifier.

For the commercial Gasification of biomass were primarily the fixed bed gasifier and the fluidized bed gasifier further developed.

From the many different technical approaches in the field of fixed bed gasification is at this point the Carbo-V process exemplified.

literature for fluidized bed gasification, which is part of this application, may be the following literature can be taken: "High-Temperature Winkler Gasification of Municipal Solid Waste ", Wolfgang Adlhoch, Rheinbraun AG, Hisaaki Sumitomo Heavy Industries, Ltd., Joachim Wolff, Karsten Radtke (Speaker), Krupp Uhde GmbH; Gasification Technology Conference; San Francisco, California, USA; October 8-11, 2000; Conference Proceedings.

literature for circulators Fluidized bed in the composite system which is part of this application, can be taken from the following literature: "Decentralized power and heat generation based on biomass gasification "; R. Rauch, H. Hofbauer; Lecture University of Leipzig 2004.

"Circulating Fluidized bed, gasification with air, Operation Experience with CfB - Technology for Waste, Utilization at a Cement Production Plant "R.Wirthwein, P. Scur, K.-F. Scharf - Rüdersdorf Cement GmbH, H. Hirschfelder - Lurgi Energy and Disposal GmbH; 7th. International Conference on Circulating Fluidized Bed Technologies; Niagara Falls, May 2002.

literature for combination Fixed bed (rotary tube), which is part of this application can from the following literature: 30 MV Carbo V Biomass Gasifier for Municipal CHP; The CHP Project for the City of Aachen, Matthias Rudloff; Lecture Paris, October 2005

literature for combination for the Fixed bed gasification (slag deadening gasifier), which is part of this Registration is, the following literature can be found: Operation Results of the BGL Gasifier at Schwarze Pumpe, Dr. med. Hans-Joachim Sander SVZ, dr. Georg Daradimos, Hansjobst Hirschfelder, Envirotherm; Gasification Technologies 2003; San Francisco California, October 12-15 2003; Conference Proceedings

at The Carbo-V process gasification takes place in two stages. First the biomass is at 500 ° C in their fleeting and solid components split. The result is a tar-containing Gas and additionally "charcoal". The gas is added Temperatures of more than 1200 ° C burned, with the tars decaying into CO2 and H2. With the hot flue gas and the charcoal will follow produces a CO and H2-containing product gas.

by virtue of of high technical and economic Expenses caused by the high pressure level (up to 40 bar), are these carburettor types for the gasification of biomass (which accumulates regionally and has significant influence on the cost of Logistics and processing has) entirely not suitable.

The Fluidized bed gasifiers can be subdivided into two processes, which is in the warm-up of the fluidized bed, the circulating fluidized bed gasifier and the stationary fluidized bed gasifier.

literature for desulfurization in a fluidized bed gasification, which is part of this application, can be found in the following literature: Gasification of Lignite and Wood in the Lurgi Circulating Fluidized Be Gasifier; Research Project 2656-3; Final Report, August 1988, P.Mehrling, H.Vierrath; Lurgi GmbH; for Electric Power Research Institute, Palo Alto, California: ZWS pressure gasification in the combi-block, final report BMFT FB 03 E 6384-A; P.Mehrling, LURGI GmbH; Bewag

In Güssing (Austria) At the beginning of 2002, it became an allothermal, circulating fluidized bed gasification plant put into operation. The biomass is in a fluidized bed with Gassing steam as an oxidizing agent. For heat supply for the gasification process Part of the charcoal produced in the fluidized bed burned a second fluidized bed. By the gasification under Steam, a product gas is generated. The disadvantages are the high ones Acquisition costs of the system technology and an excessive effort for the process control.

The management of the fluidized bed material requires a targeted control and regulation of the steam circulation in the sense of a mammoth pump movement to increase the heat and mass transfer and to improve the reaction conditions by increasing the effective reaction space. The mammoth pump is a conveying device in which solids / water mixtures with the help of compressed air (propellant or conveying gas), promoted by eg injection of this air by means of nozzles in pipes or a stirred tank becomes. The injected gas causes a reduction in the suspension density and thus an increase in buoyancy. Together with the introduced kinetic energy causes the promotion.

As a flow results in the containers a circulation flow in 2 is pictured.

It There is thus a transfer on the solid / gas suspension of the fluidized bed. This principle will in the present case to the gas / solid suspension of the fluidized bed transferred to the steam converter.

Overview of the invention:

task the invention is to provide a method and a device, optimize fluidised bed gasification.

Is solved This object is achieved by an invention having the features of the independent claims.

No known other method is capable of producing a high-quality synthesis gas at unrivaled low prices - as a result, relatively lower Investment - under the prescription of CO2 reduction, or this an energetic Use to be supplied and this at the same time - after appropriate cooling and cleaning - as To process fuel.

at In the present invention, the biomass is also in a Fluidized bed with steam as an oxidation and fluidizing medium. However, this is a stationary fluidized bed with two specially developed pulse burners, the indirect heat input allow in the reactor located in the fluidized bed.

Of the Advantage compared to the fixed bed carburetor and the circulating Fluidized bed is the absence of distinct temperature and reaction zones. The Fluidized bed consists of an inner bed material. This will be a simultaneous course of the individual partial reactions and a homogeneous temperature (about 800 ° C) guaranteed. The process is almost without pressure (up to a maximum of 0.5 bar) and is therefore technical easily implemented. It is characterized by a high economy out. The acquisition costs are among the aforementioned carburetor types.

• – Gasreinigung und CO2-Entfernung über eine Rectisol-Anlage
• – Optimierung des Verhältnisses H2 zu CO über das Shift-Verfahren
• – Fischer-Tropsch-Synthese
• – Abgabe an einen favorisierten Hydro-Cracker/Produktion Diesel mit höchstem Cetan.

The starting point for further use as fuel is the medium-calorific gas from the bio-synthesis gas plant (based on renewable raw materials), which after dedusting and scrubbing of condensable hydrocarbons (oil quench) via a turbo compressor to about 20 bar compressed and through the the following process steps can be refined:

• - Gas purification and CO2 removal via a Rectisol system
• - Optimization of the ratio H2 to CO via the shift method
• - Fischer-Tropsch synthesis
• - Delivery to a favored hydro-cracker / production diesel with highest cetane.

When The result remains to be noted that the inventive method based on the synthesis gas is capable of 100to biomass 23to produce high quality fuel.

The inventive method is characterized in that by jet nozzles the movement of the fluidized Bed can be specifically controlled and regulated. The achievable thereby Macro flow The fluidized bed, which is similar to the mammoth pump principle, serves to enlarge the reaction zone Flash pyrolysis and increase of Dwell time of the primary resulting pyrolysis coke to increase the heat and mass transfer.

These activities cause an enlargement of the effective reaction zones to increase the space-time yield and the intensification of for these secondary Perform reactions relevant, heterogeneous steam splits.

By The circulating fluidized bed is the voluminous biomass, which in the lower Part of the steam converter is accelerated, so that the reaction distance, and thus the effective reactor volume to the primary Implementation for this Reaction increased by a factor of 2 to 4.

Farther optimizes the motive nozzle the increase in the yield of CO and H2 as primary products of Steam conversion, while reducing the yield of Methane and higher Hydrocarbons.

By the change the ratio of Steam to the feed, that for the thermodynamic efficiency of the steam conversion is the Cold gas efficiency increased.

Of the Use of one or more steam jet conveyors has the task, the amount of steam required for fluidization minimize and replace some of the vapor with recycled synthesis gas, or the heat input through material heat conduction to increase from the range of impulse burners.

The unpurified synthesis gas is, due to the technology used, enriched with carbonaceous fine dust. This dust will be in a multi-stage cleaning system consisting of cyclone, multicyclone and fine filters, deposited.

The SPOT method is characterized by the fact that this dust is gravimetric or by means of jet nozzle is conveyed back into the fluidized bed. The optimal ratio between bed material and fine dust, as well as the high temperature effect, together with the high reactivity of recycled particulate matter in a heterogeneous water vapor reaction, the reaction of the coke with water vapor to CO and H2.

Essential here it is that, with the help of the Treibstrahlprinzips, the promotion of particulate matter in the dense fluidized bed is made possible, which by increase in residence time and intensive mixing of the dust with the hot bed material the required Effect improved.

Figures Description:

The Figur serves to describe the sequence of the method and the Device to better understand the following detailed To provide a description of the preferred embodiment.

1 shows the steam conversion in the fluidized bed movement by steam jet conveyor and motive nozzle.

2 shows the steam conversion fluidized bed movement by steam jet conveyors and motive nozzles.

Preferred embodiment:

The 1 shows a giver 11 with pulse burners 12 located in the middle area of the carburetor 11 are arranged to form in this area a fluidized bed or a fluidized bed, which are preferably formed stationary. The number of pulse burners can be determined variably. There are both one and two or more conceivable.

In the carburetor, steam is used as the oxidation and fluidizing medium 13 initiated. Other Fluidisiermedium, such as syngas or CO2 are also conceivable. Furthermore, starting materials 14 in the field of pulse burners 12 introduced. These feedstocks can be biomass and other substances, such as lignite or secondary raw materials (such as municipal waste, sewage sludge, waste from the food industry, etc.) The biomass is gasified in the fluidized bed, which consists of inner bed material, in the range of about 800 ° C.

The Pulse burners are operated with Q (pkt). Q (pkt) means heat flow and means the reaction enthalpy (i.e., the calorific value) of the employed Fuel gas. As fuel gas can in addition to the synthesis gas produced in the reformer (product gas) the various fuel gas streams (from propane to natural gas and the like Gases) are used, so that in particular in a plant network this Impulse burner for the combustion of so-called off-gases, which are as by-products in syntheses such as methanol synthesis, arise, are used can and thus contributes to increasing the efficiency of an entire system.

This Fuel gas comes in regular operation as a branch from the in-house production, that is the refinement of the biomass to a new product: heating gas.

In a further step, absorption or removal of chlorine, which is present as a chlorine radical and is usually derived from organic chlorine compounds, by further additives. These other additives are preferably hydrated lime or the like. These additives are preferably in the dust collector 19 . 18 or injected the multi-cyclone. Of course, it is also conceivable to inject them directly into the reactor or to add them to the starting materials.

In a further step, the dust components are separated. Here are different filters and separators 18 . 19 , connected in series. Their residues are returned to the reactor. The return can be done at different locations. Below the pulse burner 4 , or in the fluidized bed, or above the pulse burner 5 , or above the fluidized bed. Preferably, cyclones and multi-cyclones are used, as well as filters, in particular fine filters, which may be formed as a downstream battery of sintered metal filters. In a first step, a cyclone is followed, using a dust deposit 18 a return can be done below or above the pulse burner.

After that Preferably, an intermediate cooling takes place in a cooler Temperatures between 150 and 700 ° C (above the dew point of the synthesis gas), then cooled in a Multicyclone to be cleaned.

The Additive hydrated lime or similar can be supplied in both the cyclone and the multicyclone.

After that the synthesis gas will be parallel or serial to a series of fine filters fed.

The residues of the fine filters and the multicyclone are collected in a dust separator 18 . 19 , Collected and returned to the reactor at different points, as already described above. Thus, the separated dust above or below the pulse burner can be supplied. In this case, the dust can also be injected through a motive nozzle. Parts of the purified or partially purified synthesis gas are returned to the eddy current bed. In this case, preferably, a steam jet conveyor 3 used, which brings the synthesis gas in the steam. Of the 1 It can be clearly seen that the synthesis gas is recycled after the first dust separation, so it is in this case still a synthesis gas enriched with fine dust residues.

Furthermore, a motive nozzle 15 used by a controller 20 is controlled to inject the water vapor and to keep the fluidized bed in motion.

Another valve 17 serves the steam supply, whereby the steam jet conveyor is bypassed. Through the controller 21 the supply of superheated steam is determined.

The 2 shows a controlled by driving nozzles fluidized bed movement 1 and the motive nozzle with supply of the propellant.

By the fluidized bed suspension with low density is a promotion through the propellant.

The Description of the embodiments is used only for understanding this and does not intend any restrictions. The scope of protection of Invention is covered by the claims certainly.

1

Motive nozzle and controlled Fluidized bed movement

2

propelling nozzle

3

Injector / steam jet conveyor

4

dust entry in the bed "downstairs"

5

dust entry above the fluidized bed

11

Reactor, carburettor

12

pulse burner

13

fluidising

14

feedstocks

15

Drive nozzle for steam supply

16

Q (pts)

17

steam supply Bypassing of the steam jet conveyor

18

dust collector

19

dust collector

20

control the motive nozzle

21

control the feed of the overheated steam

Claims (22)

Process for the gasification of feedstocks too Synthesis gas, with a carburetor that has at least one impulse burner having a fluidized bed in the gasifier, wherein the fluidized bed by a motive nozzle, which introduces into the reactor water vapor and / or synthesis gas and / or fine dust, so held in a controlled motion that the reaction zone is enlarged. The method of claim 1, wherein the motive nozzle is below the fluidized bed is arranged. The method of the preceding claim, wherein through jet nozzles the movement of the fluidized fluidized bed controlled specifically and is regulated. The method of the preceding claim, wherein the macro flow to be achieved the fluidized bed should be similar to the mammoth pump principle, whereby the Magnification of the Reaction zone for flash pyrolysis and increasing the residence time of the primary resulting Pyrolysis coke to increase of heat and mass transfer is reached. The method according to one or more of the preceding Claims, wherein the circulating fluidized bed is controlled so that the voluminous biomass, which is introduced into the lower part of the steam converter accelerates so that the reaction distance and thus the effective Reactor volume to the primary Implementation for this reaction is preferably increased by a factor of 2 to 4. The method according to one or more of the preceding Claims, using the Treibstrahlprinzips the introduction of fine dust in the dense fluidized bed, whereby a residence time increase and intensive mixing of the dust with the hot bed material improves the reaction. A process for the gasification of feedstocks to synthesis gas, comprising a gasifier having at least one impulse burner, with a fluidized bed in the gasifier, wherein parts of Synthesega be returned to the vortex flow bed. The method of the preceding claim, wherein the synthesis gas is fed together with water vapor into the carburetor. The method of the preceding claim, wherein at least one steam jet conveyor used which introduces the syngas into the vapor. The method according to the preceding claims, wherein the use of one or more steam jet conveyors is controlled so that the amount of steam required for fluidization wherein part of the vapor is recycled by recycled synthesis gas is replaced, and / or wherein the heat input by material heat conduction is increased from the range of impulse burners. The method according to one or more of the preceding claims 7 to 10, wherein the synthesis gas is recycled only partially purified. A device for the gasification of feedstocks to synthesis gas, with a carburetor, the at least one impulse burner has, with a fluidized bed in the carburetor, characterized through a motive nozzle, in the reactor water vapor and / or synthesis gas and / or particulate matter introduces, and the controlled by means so that the fluidized bed is in motion is held so that the reaction zone is increased. The device according to the preceding claim, the driving nozzle is arranged below the fluidized bed. The device according to the preceding claim, the driving nozzles Jet Nozzle are targeted to the movement of the fluidized fluidized bed control or regulate. The device according to the preceding claim, wherein the means for control are designed so that the achieving macro flow of Fluidized bed, the mammoth pump principle is similar, whereby the enlargement of the Reaction zone for flash pyrolysis and increasing the residence time of the primary resulting Pyrolysis coke to increase of heat and mass transfer is reached. The device according to one or more of the preceding Claims, being the control of the motive nozzles is designed so that the circulating fluidized bed controlled so Will that be voluminous Biomass, which is introduced into the lower part of the steam converter is accelerated, so that the reaction distance, and thus the effective reactor volume, for primary implementation for this Reaction increased preferably by a factor of 2 to 4. The device according to one or more of the preceding Device claims, the driving nozzles Fine dust from the purification process of the synthesis gas in the dense Inject fluid bed, whereby a residence time increase and intensive mixing of the dust with the hot bed material the reaction is improved. A device for the gasification of feedstocks to synthesis gas, with a carburetor, the at least one impulse burner having a fluidized bed in the gasifier, wherein means present to parts of the synthesis gas in the Wirbelstrombett recirculate. The device according to the preceding claim, wherein there are agents to mix the synthesis gas with the To lead steam into the carburetor. The device according to the preceding claim, wherein at least one steam jet conveyor is present, the Synthesis gas in the steam brings. The device according to the preceding claims, wherein Funds are available to the use of one or more several steam jet conveyors to control so that the amount of steam required for fluidization minimized wherein part of the vapor is replaced by recycled synthesis gas, and / or wherein the heat input through material heat conduction is increased from the range of impulse burners. The device according to one or more of the preceding claims 18 to 21, wherein agents are present which the synthesis gas only partially cleaned back to lead.