WO2014180923A1 - Dispositif et procédé de traitement des condensats d'installations de gazéification - Google Patents

Dispositif et procédé de traitement des condensats d'installations de gazéification Download PDF

Info

Publication number
WO2014180923A1
WO2014180923A1 PCT/EP2014/059379 EP2014059379W WO2014180923A1 WO 2014180923 A1 WO2014180923 A1 WO 2014180923A1 EP 2014059379 W EP2014059379 W EP 2014059379W WO 2014180923 A1 WO2014180923 A1 WO 2014180923A1
Authority
WO
WIPO (PCT)
Prior art keywords
condensate
evaporation
gasification
synthesis gas
chambers
Prior art date
Application number
PCT/EP2014/059379
Other languages
German (de)
English (en)
Inventor
Thomas OEHMICHEN
Original Assignee
Krones Ag
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Krones Ag filed Critical Krones Ag
Publication of WO2014180923A1 publication Critical patent/WO2014180923A1/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/26—Multiple-effect evaporating
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/169—Integration of gasification processes with another plant or parts within the plant with water treatments

Definitions

  • the present invention relates to an apparatus and a method for the treatment of condensate, which results in the multi-stage cooling of synthesis gases from the gasification of carbonaceous starting materials.
  • the raw gas in the gasification of carbonaceous materials contains in addition to the main components H 2 , CO, C0 2 , CH 4 , H 2 0 and N 2 also undesirable trace components in the form of nitrogen compounds (NH 3 , HCN), halogen compounds (HCl, HF) or Sulfur compounds (H 2 S, COS) but also alkali metals (in particular K and Na) which are formed from the accompanying components of the raw material used.
  • the condensate takes part of the gaseous components such as C0 2 , H 2 S, S0 2 , S x , HCN, HCl and NH 3 and water-soluble hydrocarbons (phenols, organic acids) and non-water-soluble, condensing hydrocarbons on.
  • the contamination of the condensate is dependent on the concentration of the components in the gas phase, the temperature and the pH of the water.
  • AOP processes Advanced Oxidation Process
  • adsorption processes on water activated carbon for the removal of hydrocarbons
  • ion exchange, reverse osmosis and electrodeionization for desalination or adsorption on zeolites
  • stripping or MAP- Precipitation used at high ammonium concentrations.
  • GB 2 198 744 discloses the treatment of an aqueous condensate obtained in coal gasification, in which the condensate freed from solids is fed to a single-stage flash evaporation, in which the resulting vapor is recirculated as a gasification medium. Part of the brine is driven to increase the steam yield in the circuit while the other part is withdrawn from the circuit and fed to a combustion.
  • a disadvantage here proves that to achieve high concentrations, and thus lower waste streams very high circulation rates and high pumping capacities are necessary. Furthermore, the energy demand for steam generation in a single-stage flash evaporation is naturally very high. Another disadvantage turns out to be the fact that heat streams with a high temperature level are necessary to produce high-pressure steam.
  • a similar process variant is shown in the document EP 0 012 456, wherein, however, the condensate is completely passed into a flash evaporation in this, a part of the brine is used for wash cooling and only a small part of a disposal is supplied. The contaminated vapor phase is also burned.
  • a disadvantage of this method is that in the washing cooler, the sensed heat of the gas stream is converted into latent heat. Furthermore, the steam is no longer used in the process and only disposed of thermally. In addition, the high amount of wastewater proves to be disadvantageous.
  • Document DD 215 067 describes a process in which the product gas of a coal gasification under pressure is cooled in a washing cooler and condensed out in heat exchangers.
  • the condensate is subjected to a flash evaporation, wherein the resulting steam is used as a process steam via steam compressor and the brine is supplied to the wash cooler as washing water.
  • a part of the sump in the expansion tank is removed and disposed of.
  • the disadvantage in particular, is the energy-intensive circulation resulting from the low vapor yield, as well as the high expenditure on apparatus and energy for vapor compression.
  • the present invention is therefore based on the object, the treatment of an aqueous condensate obtained in the multi-stage direct and indirect cooling of this raw gas over the known from the prior art method to improve, so that in particular the purified water in the process, such as Generation of high-pressure process steam, can continue to be used. There should be as few waste streams as possible.
  • Another object of the invention is a concentration of impurities, so that it is possible to recover them as recyclables.
  • Another object of the present invention is to provide a highly energy efficient and flexible process which allows the use of low to medium temperature waste heat and which is suitable or readily adaptable to various gasification processes with a variety of carbonaceous feedstocks and, consequently, different condensate compositions. Also, the need for auxiliaries should be reduced to a minimum.
  • the plant according to the invention for the gasification of carbonaceous fuels to synthesis gas comprises a gasification device and is characterized in particular by the fact that the system comprises a multi-stage evaporation device wherein the evaporation device has at least one heating device for the condensate in which the condensate at a predeterminable pressure on a predeterminable Temperature can be heated and the evaporation device comprises a plurality of chambers and at least one heat exchanger and through these chambers heated by the heating device condensate - in particular in countercurrent - to the conductive heating condensate feasible, in which chambers the heated condensate by flash evaporation at least partially in the gaseous state can be converted and the resulting gaseous medium is fed to a heat exchanger for heat transfer to the condensing device to the heating means, wherein the gaseous medium in the heat exchanger to form a distillate to a predetermined temperature and in particular a temperature below the boiling point is cooled and in the liquid state from the heat
  • the condensate directly after its condensation still has the boiling point and preferably takes place by further heat losses in the system further cooling to a temperature below the boiling point.
  • the plant has a cleaning device for the synthesis gas downstream of the gasification device in particular, wherein the vaporization device is preferably connected to the cleaning device in such a way that condensate accumulating in the cleaning device can be supplied to the vaporization device.
  • the gasification device downstream purification device for the synthesis gas a preconditioning of the crude gas stream and thus a pre-cleaning of the condensate should be achieved.
  • This is intended to bring about a reduction of the dust and tar content, in particular with high dust loads and / or high tar loadings. Without separation, these would cause considerable problems in gas side downstream equipment such as heat exchangers and condensers.
  • hot gas cyclones or hot gas filters based on ceramic or metallic materials can be used.
  • thermal and / or catalytic crackers are suitable, since these convert the tars into valuable gas components such as CO and H 2 .
  • the tars can be used in downstream processes both energetically and materially.
  • the handling and processing of the condensate is considerably improved by the present invention of the gasification device downstream cleaning device for the synthesis gas, as this, as already illustrated, represent difficult to process media.
  • Preferred is a system which has means by which the condensate can be pre-cleaned in the gaseous state before cooling.
  • the pre-purification means preferably comprises means for removing solids from the gas.
  • the pre-cleaning means comprise means for removing tar compounds from the gas.
  • this device is suitable for converting the tar compounds primarily into hydrogen, carbon monoxide and short-chain hydrocarbons.
  • the pre-cleaned by means of a device for pre-cleaning gas stream is fed to a multi-stage gas cooling.
  • the inlet temperature of the raw gas depends on the gasification technology used, but is often above the tar condensation temperature, since this avoids fouling and clogging of piping and equipment.
  • the temperature after cooling depends on the desired water vapor content and the gasification pressure. Another significant factor determining the cooling temperature is the tarmac required for the process.
  • a gas scrubber is integrated to increase the mass transfer area. In this, the gas stream is brought back into contact with part of the condensate.
  • a scrubber advantageous jet or Venturi scrubber can be used. These also offer the advantage of fine dedusting.
  • a second wash consisting of packed columns or tray columns of the first washing stage can be connected downstream.
  • the system preferably has a separating device, by means of which the solids contained in the condensate as well as all substances not dissolved in the water, such as oil droplets, can be separated off. These leave as a waste stream the separation apparatus and can either be returned to the gasifier, be sent to incineration or disposed of.
  • a separating device by means of which a part of the liquid issuing from the evaporation device can be combined with the condensate produced in the cleaning device and again into the evaporation device is feasible and another part of the liquid emerging from the evaporation device from the plant can be discharged.
  • Another essential aspect of the present invention is a process for treating condensate from gasification of carbonaceous fuels to synthesis gas in a plant for gasification of carbonaceous fuels to synthesis gas, wherein the condensate is formed in a cooling and purification of the synthesis gas, characterized in that the Condensate a multi-stage evaporator with multiple, ie at least two chambers, at least one heat exchanger and at least one heating device for the condensate is supplied, wherein the condensate is heated in the heating device at a predeterminable pressure to a predetermined temperature and then fed to one of the chambers in countercurrent to the condensate flowing to the heating device in which at least partial evaporation of the condensate takes place by flash evaporation and in which the resulting gaseous medium is used to heat a heat exchanger for heating the condensate flowing to the heating device and at least partially liquefies to form a distillate.
  • the condensate is passed through at least one heat exchanger of the evaporation device to the heating device, brought there to a predeterminable elevated temperature and - especially in the opposite direction - again supplied to the evaporation device, wherein therein (and after the increase in the condensate temperature by the heating device) the evaporation of the condensate by means of flash evaporation and the evaporation takes place in several ie at least two stages.
  • the condensate is preferably supplied stepwise to a multiplicity of expansion chambers, with one part of the condensate or its solvent (eg (and usually mostly water) evaporating) and the remaining liquid or brine (sump) being further evaporated Evaporation is fed into the next relaxation room.
  • the resulting vapor is preferably deposited in each stage (chamber) of capacitors and discharged as a condensed liquid or distillate.
  • capacitors are preferably designed as heat exchangers in some chambers, particularly preferably all chambers, by means of which the condensate flowing to the heating device can already be pre-tempered (ie, heated).
  • the heat for the final heating of the condensate in the heating device is discharged directly or indirectly from processes which cause cooling of the synthesis gas.
  • the discharged distillate has an elevated temperature, it is preferable to use it as feedwater for the production of process steam. It may be necessary to pre-heat the distillate before use as feed water.
  • the heat can be used, which arises in the inventive cooling of the raw gas gasification.
  • the energy for the evaporation is provided for the purposes of the invention from the heat of reaction of the reaction of the synthesis gases.
  • a portion of the condensate not evaporated in the chambers during the flash evaporation is removed from the evaporator and is combined with the condensate formed during the cooling and purification of the synthesis gas and passed again into the evaporation device and another part of the not evaporated in the chambers in the flash evaporation condensate is discharged from the plant.
  • a part of the liquid emerging from the last evaporator stage is preferably again pressurized and through at least a portion of the preheater stages and the final heater again led to the first evaporator stage.
  • the mixing of circulating water and condensate can take place outside of the relaxation room in a separate vessel or advantageously in the last expansion stage.
  • the condensate is degassed. Escaping gases are preferably removed via corresponding devices (eg valves).
  • the condensate is preferably stripped before evaporation (with steam or otherwise). Stripping preferably takes place in situ by flash evaporation.
  • the condensate flowing through the preheating and the final heater be brought to an elevated pressure, which is above the vapor pressure of the condensate after the final heater.
  • this pressure should also be above the vapor pressure associated with the inlet temperature of the heating medium flowing into the final heater.
  • the pressure increase is preferably carried out at the latest at a point which is below the point at which the condensate begins to boil. Since vaporization leads to an accumulation of dissolved salts and other substances which are not vaporizable under the process conditions, supersaturation can cause the formation of local material deposits. To counteract this, it is provided that preferably a certain proportion of the brine is continuously removed from the process.
  • the maximum degree of thickening is mainly determined by the raw material to be gasified and the gasification process.
  • the salt load and chemical composition of the condensate can therefore vary greatly from process to process. In principle, a high concentration should be striven for, since fewer waste streams are produced. However, the maximum concentration is coupled to the least soluble salt. It is known that, in particular, salts of Al, Ca, Mg, F, Fe and Si cause deposits, with Si0 2 , CaF 2 , MgF and iron cyanide in particular being classified as problematic.
  • the salt gradient over the number of stages is to be set so that no precipitation occurs in the evaporation chambers but only after the last stage in the brine effluent.
  • the discharged brine can be fed to further process steps. If the calorific value is sufficiently high, oil or gas assisted combustion is possible. Alternatively, brine streams can be sent for disposal.
  • the dissolved salts can be recovered from the brine. Preference is therefore given to a process variant in which the condensate not evaporated in the chambers during the flash evaporation is subjected to a value added of the salts contained therein.
  • the advantages of the multi-stage compared to a single-stage flash evaporation are that at constant total temperature difference or constant pressure difference between the incoming pressure water and the effluent from the last stage brine, i. with the same energy content, a higher steam or distillate yield is possible, which also leads to lower circulation rates. Furthermore, an increase in the number of stages leads to improved heat recovery during condensation and thus to a lower heat requirement during final heating.
  • Non-condensable constituents can accumulate.
  • the presence of such compounds reduces the efficiency of vapor condensation, as they form a kind of insulating layer around the heat exchangers in the capacitors due to their low thermal conductivity.
  • gas components must be removed from the chambers, which can be realized, for example, with the aid of a blower.
  • Non-condensable compounds include above all volatile hydrocarbons and physically dissolved gas constituents of the synthesis gas. Because of the still existing calorific value, these can advantageously be subjected to combustion. With the help of a blower, it is also possible to set a negative pressure in the last chamber, so that temperatures of less than 100 ° C are possible in the brine.
  • Thermo oils, superheated low and high pressure steam or saturated steam can be used as the heat transfer medium for the final heating of the condensate. It must be taken into account here that the temperature difference between the exiting condensate and the incoming heating medium is minimized, since otherwise very high pressures in the condenser would occur. would require. Particularly advantageous is the use of saturated steam, as this ensures a very good heat transfer in addition to a very uniform temperature distribution in the heating circuit. As a heat source can advantageously be used, the waste heat, which is obtained during the cooling of the gas stream of the gasification.
  • the inlet temperature of the condensate into the expansion chambers of the evaporator is a process-specific parameter. In the sense of a high distillate yield per passage and consequently lower circulation rates and pumping costs, a high temperature level should be aimed for. If the final heating is not carried out with additional fuel but with waste heat from the process, the upper limit is limited by the temperature level of existing waste heat flows. Another important point arises from the decreasing solubility of some salts with increasing temperature. These include compounds such as CaS0 4 , CaC0 3 or Mg (OH) 2 which also have a very low solubility. In this case, the temperature range and the concentration of the salts should be adjusted so that no precipitation takes place during the heating.
  • the dissolved salts remain on evaporation in the brine, so as to ensure that entrained liquid droplets are retained by the vapor phase.
  • corresponding devices such as, for example, droplet separators in the form of demistors, are provided.
  • the brine contains all high-boiling organic compounds.
  • the vapor phase which is virtually free of halogens, consists of the more volatile organic constituents, ammonia (NH 3 ), hydrogen sulphide (H 2 S) and gases physically dissolved in the condensate.
  • the vapor fraction may still contain portions of HCN.
  • the distillate is used for the production of process steam.
  • the recovered distillate can be used in evaporators to recover high pressure process steam.
  • the waste heat or reaction heat of reactions of the synthesis gases such as methanol production, methanation, Fischer-Tropsch synthesis or ammonia synthesis can be used as a heat source for steam generation.
  • Particularly preferred is a process variant in which the process steam is used as a gasification agent for the gasification of the carbonaceous fuels.
  • the recovered high-pressure steam is used as a gasification agent for the gasification process, it can be exploited that contamination of the steam by NH 3 , HCN or volatile hydrocarbons then plays a subordinate role due to the further use and the resulting chemical reactions.
  • Ammonia is partially broken down into its elements in the gasifier or tar cracker, HCN can be hydrolyzed, and the hydrocarbons are reformed.
  • Preference is given to a process in which reaction heat of reactions of the synthesis gas is used for the purpose of generating steam. As a result, a particularly efficient thermal utilization of the heat of reaction of reactions of the synthesis gas is possible.
  • a purification of the synthesis gas is carried out. It is possible that certain components are filtered out during this cleaning.
  • This tar separation can also be effected by a cracking or cracking of tar.
  • a purification of the condensate is carried out. In particular, this cleaning of the condensate is fed before it is fed to the system.
  • Fig. 1 a flow chart of the method
  • FIG. 1 illustrates, by way of example, a possible flow diagram of the process.
  • the carbonaceous starting material 2 is introduced into a gasification reactor 1, eg, a gasification reactor 1.
  • B aellesfest- bed gasifier or a fluidized bed gasifier introduced, in which it is reacted with the gasification agent 3.
  • the resulting ash 4 is removed from the reactor.
  • the product gas consisting of the gaseous reaction products, unreacted gasification agents, dust and aerosol-shaped and / or liquid tars and other constituents, is led out of the gasifier via line 5 and introduced into a dedusting device 6.
  • measures according to the prior art such as hot gas cyclones and / or hot gas filters (eg bulk material filters, ceramic filters or metal filters) can be used.
  • the separated dust / solid 7 can be disposed of. If the dust consists largely of unreacted biomass particles, a return of these in the carburetor (not shown) is advantageous.
  • FER ner the gas is supplied to a Entte für assusky.
  • the tars can be separated, for example, by condensing over the line 10.
  • By supplying heat 9 and / or by adding oxygen-containing gases 9 and associated partial oxidation endothermic cracking and reforming reactions are enabled, by which the tars are converted into more valuable gas constituents such as H 2 and CO be implemented.
  • adsorptive or absorptive processes can also be used for tar removal.
  • the pre-cleaned, so dedusted and entteerte gas is fed to a multi-stage gas cooling.
  • the gas stream is cooled. It is also possible in a further embodiment of the invention that more than two cooling stages are used.
  • the cooling temperature depends on the desired water vapor content and the gasification pressure. If, for example, the gas is to be dried to a water content of 0.5% by volume, the gas must be cooled to 2 ° C.
  • the water-soluble gas constituents and impurities such as, for example, HCl
  • the gas cooling is combined with gas scrubbing.
  • the gas is first introduced in a Venturi or free-jet scrubber 13, in which an additional fine dedusting takes place.
  • the gas passes through a further scrubber 14, which may consist of a packed body or tray column. It may be advantageous in this case to add a pH-increasing or decreasing fluid to the washing medium via the line 15, so that the separation efficiency in the second scrubber 14 is improved.
  • At least partially pre-cleaned condensate is used in all the scrubbers in this preferred embodiment.
  • the discharged condensate which is obtained depending on the process conditions at a temperature of 30 to 200 ° C, is fed to a treatment 16, in which all components not dissolved in the water such as dust particles and oil drops are separated and removed via line 17 from the system.
  • a treatment 16 in which all components not dissolved in the water such as dust particles and oil drops are separated and removed via line 17 from the system.
  • These can be disposed of, advantageously subjected to combustion or, particularly advantageously, returned to the gasification apparatus (not shown).
  • sedimentation or flotation can be used for very fine solids flocculation can be used in addition.
  • a portion of the pre-cleaned condensate can be added via the line 18 by means of the pump 19 to the scrubbers 13 and 14 as a washing medium.
  • the remaining part is fed via a feed line 20 by means of a pump 21 to an evaporation unit 23, which consists of a plurality of individual chambers k-k- n .
  • the condensate is mixed in a pre-mixer 22 with a circulated from the evaporator and concentrated liquid 28 and preheated and further heated by a plurality of heat exchanger 24 and a final heater 25, in which a heating to a temperature of 120 to 320 ° C. takes place.
  • the thus heated condensate and the heated circulation stream are successively several chambers k- ⁇ - k n fed, in which each evaporates a portion of the stream by flash evaporation, and the non-evaporated part, the brine, the next chamber is added, in which another evaporation takes place.
  • the resulting vapor stream is condensed at heat exchangers 24 and removed as distillate 27 at a temperature of 40 to 200 ° C and a pressure of 0.1 to 16 bar (a) by means of a pump 26 from the evaporator and made available to other applications.
  • the released latent heat is, as described, used for preheating.
  • a part of the non-evaporated brine leaving the last stage is pressurized again at a temperature of 45 to 210 ° C. and a pressure of 0.1 to 19 bar (a) by means of a pump 29 and Premixer 22 mixed with the condensate 20 and cooled and fed through the heat exchanger 24 and the end heater 25 again to the evaporation process.
  • the non-recirculated part of the brine 31 is removed from the system and can be made available to further process steps (not shown). If the calorific value is sufficiently high, an oil or gas-assisted combustion. Otherwise, another disposal is necessary.
  • the salts dissolved in the brine which consist mainly of ammonium chloride in the case of chlorine-containing feedstocks, can be recovered.
  • crystallizers or dryers are suitable (not shown).
  • thermo-technical relationship between the distillate temperature and the temperature of the inflowing condensate in the evaporator, wherein the condensate temperature should always be less than the distillate temperature.
  • This temperature difference must be the greater the higher the temperature span between the final heater and the last evaporation chamber, the greater the return rate and the smaller the number of evaporator stages. Since even in the multi-stage flash evaporation no complete heat recovery is possible, this excess heat from the evaporation process is largely removed and used to preheat the condensate. Another waste heat flow is the separated brine. If the requirements of the process are such that this minimum temperature difference can not be guaranteed, the heat must be removed from the circuit otherwise. This can be realized, for example, by cooling the recirculated brine prior to addition to the premixer 22 by means of a heat exchanger (not shown).
  • the pressure increase by the pumps 21 and 29 must be so high that the pressure after the increase is greater than the vapor pressure of the condensate after the final heating 25, and advantageously greater than the vapor pressure of the condensate at the temperature with which the heating medium flows into the final heater.
  • Typical pressures are in the range of at least 2 bar to 100 bar (g).
  • non-condensable compounds may accumulate in the chambers of the evaporator.
  • a blower 32 with which it is also possible to set a negative pressure in the system, so that brine temperatures below 100 ° C are possible.
  • discharge valves can be used in process overpressure.
  • the vented gases can be disposed of thermally in a combustion chamber 33. It is therefore advantageous to pretreat the condensate for the purpose of degassing before entering the premixer (not shown). For this purpose, stripping methods (with steam or other gases).
  • the condensate at elevated temperature of a partial pre-evaporation by flash evaporation (in situ stripping) are subjected.
  • non-condensable dissolved gases and other volatile substances for example, some ammonium salts
  • This step can also be used to reduce the temperature in the condensate, for. B. to allow lower distillate temperatures.
  • the composition of the vapor phase can be adjusted.
  • Setting the pH above 10 to 12 prevents cyanides from entering the vapor.
  • the condensate may be supplied via line 34 with a pH-increasing medium, e.g. Sodium hydroxide solution can be added.
  • the distillate can be heated in a preheater 35 and used as feed water for a steam generator 36 for generating process steam 38, wherein the waste heat of a chemical reaction of the synthesis gas 37 is used as heat of vaporization.
  • FIG. 2 shows a process variant in which the degassing of the condensate is integrated in the evaporator.
  • the evaporator in the process shown in Figure 1 consists of only a part with a plurality of chambers k- ⁇ - k n , in which the heat is recovered
  • the evaporator shown in Figure 2 consists essentially of a heat recovery part 40 with a plurality to chambers n-n n and a cooling part 39 having a multiplicity of chambers mi n m.
  • the condensate is passed through the condensate line 41 and a pump 42 through the heat exchanger tubes 49 of the cooling part, wherein a partial flow via the line 43 and corresponding pump 44 and if necessary additionally by a heat exchanger not shown the line 18 is added and the other part via a Feed line 45 is placed in the last chamber of the heat recovery part, whereby a mixing takes place with the recirculated concentrated brine.
  • the degassing of the condensate in the last stage is made possible, so that a separate premixer 22, as shown in FIG. 1, can be saved.
  • the inlet temperature of the condensate in the last stage of the cooling part is at the same level as the temperature of the brine in the last stage of the cooling section.
  • the common stream of condensate and brine is brought from the last stage of the cooling part by means of a pump 46 to an elevated pressure, passed through line 47 through the heat exchanger tubes 48 of the heat recovery part 40 and brought in an end heater 25 to an elevated temperature.
  • the thus heated stream is successively several chambers n-n n of the heat recovery section and then several chambers mi n m supplied to the cooling part, in which each part of the stream evaporated by flash evaporation, and the non-evaporated part, the brine, the next chamber is added, in which a further evaporation takes place.
  • the resulting vapor stream is condensed at heat exchangers 48 and the heat exchangers 49 and led out as distillate 27 at a temperature of 40 to 200 ° C and a pressure of 0.1 to 16 bar (a) via the pump 26 from the evaporator ,
  • the liberated latent heat is used in the heat recovery part for preheating the recirculated brine and the condensate stream and used in the cooling part for preheating the condensate. From the last stage of the cooling part, excess brine can be removed from the circuit via the pump 31 and the line 30.
  • the pressure increase with the pump 42 should be such that the condensate does not start to boil in the heat exchangers 49 and the pressure after the heat exchangers is greater than the pressure in the last chamber of the cooling part.
  • the pressure after the increase is greater than the vapor pressure of the condensate after the final heating 25, and advantageously greater than the vapor pressure of the condensate at the temperature at which the heating medium flows into the final heater.
  • Typical pressures are in the range of at least 2 bar to 100 bar (a).
  • the cooling part can accumulate non-condensable gases. These are drawn off by means of a blower 32 from this and preferably disposed of thermally in a combustion chamber 33.
  • the blower can be replaced by a discharge valve at process overpressure.
  • appropriate discharge devices can also be provided in some previous chambers.
  • the condensate pH By adjusting the condensate pH, the composition of the vapor phase can be adjusted. Setting the pH above 10 to 12 prevents cyanides from entering the vapor.
  • the condensate (analogous to the variant shown in FIG. 1) can be added via line 34 to a pH-increasing medium.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Industrial Gases (AREA)

Abstract

La présente invention concerne une installation et un procédé de traitement des condensats de la gazéification de combustibles carbonés dans une installation de gazéification servant à produire du gaz de synthèse, les condensats résultant du refroidissement et de l'épuration du gaz de synthèse, caractérisé en ce que les condensats sont introduits dans un système de vaporisation multi-étages comportant plusieurs chambres, au moins un échangeur thermique et au moins un système de chauffage des condensats. Sous une pression prédéfinissable, le système de chauffage chauffe les condensats à une température prédéfinissable. Ceux-ci sont ensuite envoyés dans une des chambres, à contre-courant des condensats arrivant au système de chauffage, où une distillation éclair provoque une vaporisation au moins partielle des condensats et où le milieu gazeux résultant est utilisé dans un échangeur thermique pour chauffer les condensats qui arrivent au système de chauffage et se liquéfient au moins en partie en formant un distillat.
PCT/EP2014/059379 2013-05-10 2014-05-07 Dispositif et procédé de traitement des condensats d'installations de gazéification WO2014180923A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102013104828.5A DE102013104828A1 (de) 2013-05-10 2013-05-10 Vorrichtung und Verfahren zur Behandlung von Kondensat aus Vergasungsanlagen
DE102013104828.5 2013-05-10

Publications (1)

Publication Number Publication Date
WO2014180923A1 true WO2014180923A1 (fr) 2014-11-13

Family

ID=50678212

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2014/059379 WO2014180923A1 (fr) 2013-05-10 2014-05-07 Dispositif et procédé de traitement des condensats d'installations de gazéification

Country Status (2)

Country Link
DE (1) DE102013104828A1 (fr)
WO (1) WO2014180923A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114146586A (zh) * 2021-12-30 2022-03-08 苏州金宏气体股份有限公司 一种氢氟酸溶液的配置装置及方法
DE102023121731A1 (de) 2023-08-14 2023-10-05 Thyssenkrupp Ag Verfahren zur Rückgewinnung von Prozesskondensat

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2007149879A2 (fr) * 2006-06-19 2007-12-27 Energy & Environmental Research Center Foundation Procédé et appareil pour améliorer la qualité de l'eau au moyen de la gazéification
GB2443802A (en) * 2006-11-08 2008-05-21 L E T Leading Edge Technologie Thermal desalination plant integrated upgrading process and apparatus
US20090152208A1 (en) * 2007-12-12 2009-06-18 Agrawal Ravindra K Method for treatment of process waters using steam
EP2246531A1 (fr) * 2009-04-30 2010-11-03 Alstom Technology Ltd Centrale électrique avec capture du CO2 et purification d'eau
US20110162952A1 (en) * 2010-01-07 2011-07-07 General Electric Company Salt water desalination using energy from gasification process

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3574066A (en) * 1968-02-19 1971-04-06 Kurita Industrial Co Ltd Multistage evaporation unit and gasliquid direct contact distillation apparatus
DE2853989C2 (de) 1978-12-14 1980-07-31 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zum Behandeln von wasserhaltigem Kondensat aus der Kühlung des Rohgases der Druckvergasung
DD215067A1 (de) 1983-05-12 1984-10-31 Schwarze Pumpe Gas Veb Verfahren zur verringerung des phenolwasseranfalls bei der kohledruckvergasung
DE3515484A1 (de) 1985-04-30 1986-10-30 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zum behandeln von kondensat aus dem produktgas der vergasung fester brennstoffe
DD260619A3 (de) * 1986-08-11 1988-10-05 Piesteritz Agrochemie Verfahren zur kesselspeisewassererzeugung durch rauchgasabwaermenutzung
GB8630047D0 (en) 1986-12-16 1987-01-28 British Gas Plc Purification of effluent liquors
DD262168A1 (de) * 1987-07-01 1988-11-23 Piesteritz Agrochemie Verfahren zur kesselspeisewassererzeugung mittels absorptionswaermepumpenprozess
US6086722A (en) 1996-07-17 2000-07-11 Texaco Inc. Minimizing evaporator scaling and recovery of salts during gasification

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2007149879A2 (fr) * 2006-06-19 2007-12-27 Energy & Environmental Research Center Foundation Procédé et appareil pour améliorer la qualité de l'eau au moyen de la gazéification
GB2443802A (en) * 2006-11-08 2008-05-21 L E T Leading Edge Technologie Thermal desalination plant integrated upgrading process and apparatus
US20090152208A1 (en) * 2007-12-12 2009-06-18 Agrawal Ravindra K Method for treatment of process waters using steam
EP2246531A1 (fr) * 2009-04-30 2010-11-03 Alstom Technology Ltd Centrale électrique avec capture du CO2 et purification d'eau
US20110162952A1 (en) * 2010-01-07 2011-07-07 General Electric Company Salt water desalination using energy from gasification process

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114146586A (zh) * 2021-12-30 2022-03-08 苏州金宏气体股份有限公司 一种氢氟酸溶液的配置装置及方法
CN114146586B (zh) * 2021-12-30 2023-11-21 金宏气体股份有限公司 一种氢氟酸溶液的配置装置及方法
DE102023121731A1 (de) 2023-08-14 2023-10-05 Thyssenkrupp Ag Verfahren zur Rückgewinnung von Prozesskondensat

Also Published As

Publication number Publication date
DE102013104828A1 (de) 2014-11-13

Similar Documents

Publication Publication Date Title
EP2262875B1 (fr) Procédé et dispositif de traitement de flux de fluides apparaissant lors de la gazéification
CH702522A2 (de) Salzwasser-Entsalzungssystem und Verfahren unter Einsatz von Energie aus einem Vergasungsverfahren.
DE102007035301B4 (de) Verfahren und Vorrichtung zur Verwertung von bei der biologischen Aufbereitung von Gaskondensat anfallender Salzlauge
DE2726302A1 (de) Verfahren und anlage zur reinigung von abwaessern
EP2388305A2 (fr) Utilisation thermique de carburants solides
EP3235784B1 (fr) Procédé et installation pour la production d'hydrogène par vaporeformage catalytique d'un gaz d'alimentation contenant des hydrocarbures
WO2014180923A1 (fr) Dispositif et procédé de traitement des condensats d'installations de gazéification
DE102009012556B4 (de) Vorrichtung und Verfahren zur Vorwärmung des Kreislauf-Quenchwassers für einen Vergasungsprozess
WO2012149988A1 (fr) Procédé de gazéification d'une matière de départ solide contenant du carbone
EP3305724A1 (fr) Procédé permettant d'obtenir du phosphore
DE2735090A1 (de) Verfahren zur herstellung von wasserstoff und kohlenoxid enthaltenden prozessgasen
WO2014195110A1 (fr) Installation et procédé de traitement d'eau
DE102007027397B4 (de) Verfahren zum Kühlen eines Wasserstoff und Wasserdampf enthaltenden Prozessgases aus einer Wasserstoffgewinnungsanlage
DE102014113307A1 (de) Reaktor und Verfahren zur Erzeugung eines Brenngases aus mechanisch entwässertem Schlamm
WO2008141784A2 (fr) Procédé de refroidissement d'un gaz de processus renfermant de l'hydrogène et de la vapeur d'eau, issu d'une installation de production d'hydrogène
DE4230266A1 (de) Verfahren und Vorrichtung zur Wärmerückgewinnung beim chemischen Abbau von Klärschlamm oder Abwasser
DE102012013139B4 (de) Verfahren und Vorrichtung zur Vergasung von Feststoffen
DE3941431C2 (de) Verfahren und Anlage zur Deponiegas- und Sickerwasserentsorgung
DE102010050495A1 (de) Verfahren und Anlage zur Herstellung von Aluminiumoxid aus Aluminiumhydroxid
DE102008051058B4 (de) Verfahren zur Abtrennung von festen Partikeln aus einer Wasserphase in einer Anlage zur Erzeugung von Kohlenwasserstoffen
DE102023121731A1 (de) Verfahren zur Rückgewinnung von Prozesskondensat
AT389466B (de) Verfahren und anlage zur thermischen behandlung von guetern mit feststoffanteil
DD205805A1 (de) Verfahren und vorrichtung zur rohgasreinigung und -abkuehlung
AT390245B (de) Verfahren zur gewinnung und/oder entfernung von in waessern, wie organisch belasteten abwaessern, enthaltenen stoffen
WO2012034662A1 (fr) Procédé de purification de condensat de traitement

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 14721899

Country of ref document: EP

Kind code of ref document: A1

122 Ep: pct application non-entry in european phase

Ref document number: 14721899

Country of ref document: EP

Kind code of ref document: A1