WO2001025143A1 - METHOD AND APPARATUS FOR SYNTHESIS OF HCl - Google Patents

METHOD AND APPARATUS FOR SYNTHESIS OF HCl Download PDF

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Publication number
WO2001025143A1
WO2001025143A1 PCT/NO2000/000313 NO0000313W WO0125143A1 WO 2001025143 A1 WO2001025143 A1 WO 2001025143A1 NO 0000313 W NO0000313 W NO 0000313W WO 0125143 A1 WO0125143 A1 WO 0125143A1
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WO
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Prior art keywords
hcl
gas
steam
gas cooler
synthesis
Prior art date
Application number
PCT/NO2000/000313
Other languages
French (fr)
Inventor
Hans Ragnar Eklund
Per Bjørn ENGSETH
Birger Langseth
Jan Sandviknes
Tore S. Pettersen
Bengt M. RØNNEVIG
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Norsk Hydro Asa
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Filing date
Publication date
Application filed by Norsk Hydro Asa filed Critical Norsk Hydro Asa
Priority to AU76928/00A priority Critical patent/AU7692800A/en
Publication of WO2001025143A1 publication Critical patent/WO2001025143A1/en

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B7/00—Halogens; Halogen acids
    • C01B7/01—Chlorine; Hydrogen chloride
    • C01B7/012—Preparation of hydrogen chloride from the elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J10/00—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B7/00—Halogens; Halogen acids
    • C01B7/01—Chlorine; Hydrogen chloride
    • C01B7/07—Purification ; Separation
    • C01B7/0706—Purification ; Separation of hydrogen chloride
    • C01B7/0731—Purification ; Separation of hydrogen chloride by extraction
    • C01B7/0737—Purification ; Separation of hydrogen chloride by extraction hydrogen chloride being extracted
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00002—Chemical plants
    • B01J2219/00004—Scale aspects
    • B01J2219/00006—Large-scale industrial plants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
    • B01J2219/00094—Jackets
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

Definitions

  • the invention concerns a method and an apparatus for the synthesis of hydrogen chloride with increased and high value energy recovery.
  • the reaction mixture is combusted in a substantially hollow, cylindrical furnace, in the course of which considerable quantities of heat are produced .
  • the hydrogen chloride gas produced is cooled and generally absorbed by water in an absorber that follows.
  • the furnace used for performing the synthesis is usually made of graphite.
  • German Patent No. DE-PS 33 13 761 it is known to cool hydrogen chloride gas in a first heat exchanger to approximately 200 °C with water carried in a circulation loop, to extract some of the absorption heat in a second heat exchange, and to effect flash evaporation of at least some of the heated water in heat exchange with the first.
  • steam is produced at a temperature of approxi- mately 138° C and a vapour pressure of approximately 350 kPa which can be used industrially for instance as process steam.
  • German patent No. DE-PS 38 07 264 discloses a method and apparatus for generating saturated steam by the combustion of chlorine and hydrogen to produce hydrogen chloride gas.
  • the apparatus includes an elongated synthesis furnace having an upper segment, a lower segment and a middle segment having a wall in the form of a heat exchanger.
  • a heat transfer medium is circulated between the heat exchanger and a steam generator while heating the heat transfer medium to between 170° and 230 °C by heat exchange between the heat of the combustion and the heat transfer medium.
  • Saturated steam is generated from water at a pressure of at least 700 kPa in the steam generator.
  • the object of the present invention is to increase the production capacity of HCl per unit. Another object is to recover produced energy efficiently at a higher temperature and pressure level than possible earlier. It is also an object of the invention to find more durable materials of construction which will result in less maintenance costs and longer life.
  • the invention thus concerns a method for the synthesis of HCl with energy recovery, where hydrogen and chlorine is supplied to a cooled synthesis furnace with a burner section and the produced HCl gas is absorbed in water.
  • the cooling water for the synthesis furnace is used for production of steam.
  • the energy is recovered as steam at a pressure above 2.8 MPa.
  • the HCl gas is further cooled in a gas cooler before the gas is absorbed in water.
  • a gas cooler of the convective type is used where the HCl gas flows through the tube side of the gas cooler.
  • the cooling water for the gas cooler as well as the burner section is integrated in the steam generating system.
  • the invention also includes an apparatus for the synthesis of HCl with energy recovery comprising a burner section, a combustion chamber, an absorber and a steam generator, wherein a gas cooler is arranged between the combustion chamber and the absorber.
  • a gas cooler of the convective type is used where the HCl gas flows through the tube side of the gas cooler.
  • the wall of the combustion chamber constitutes a heat exchanger made up of vertical tubes connected with bars preferably fixed off the centerline between the tubes. It is preferred to use construction materials of alloy with a high Ni content.
  • the apparatus is essentially made of graphite or steel, and this leads to limitations concerning the quality of recovered energy, i.e. vapour temperature and pressure. Furthermore, the method of producing the graphite elements sets a limitation with regard to the maximum size of the separate units of the furnace that can be manufactured.
  • Figure 1 shows a HCl synthesis reactor with integrated heat recovery system.
  • Figure 2 A shows a wall of the combustion chamber with center welded bars.
  • Figure 2B shows a wall of the combustion chamber with off-center arrangement of flat bars.
  • the gas cooler 4 used is preferably of a convective type, and the hydrogen chloride gas should flow through the tube side of the cooler.
  • the heat generated in the synthesis process is removed by circulating pressurized water and recovered as energy in steam at high temperature and pressure. Water is circulated between the heat exchanger forming the wall of the combustion chamber and a steam generator (steam drum) 9 where steam is produced.
  • the cooling water for the gas cooler 4 is also integrated in the steam generating system, thereby giving increased energy recovery.
  • heat is also recovered from the burner section 1 as an integrated part of the steam generation system.
  • the wall of the combustion chamber 3 forms a heat exchanger and is made up of vertical tubes 10, for circulation of water, that are interconnected by flat bar strips 11.
  • a conventional arrangement is to have the flat bars center to center between the tubes. This is illustrated in Figure 2A. Due to varying stress in the bar and tube, there will be axial strain in the middle of the bar and the inner part of the tubes, and stress at the outer side of the tubes.
  • FIG. 2 B An alternative construction is shown in Figure 2 B where the bars are welded off the centerline between the pipes.
  • the advantage of the latter arrangement is higher mechanical strength of the wall due to lower heat stress at a given heat load. Thereby the temperature differences in bars and pipes are reduced, and the heat recovered by the cooling medium will increase.
  • the manufacture is less complicated, since the tube wall needs welding on only one side, in contrast to the center arrangement where welding on both sides is required.
  • the combustion chamber can withstand a 25 kPa(g) inner reactor pressure when flat bars are welded centric to the tubes. With the flat bars welded off-centre, the construction can withstand 50 kPa(g) inner pressure due to less thermal stress on the flat bars. By putting buck stays at two meters distance around the reactor, the explosion pressure can be 2 barg in the reactor without serious damages to the construction.
  • the Incoloy ® alloys may be borderline with respect to economic feasibility (cost of installation/ life expectancy) due to their relatively low Ni content of 30-40 %.
  • the Inconel ® alloy is considered more optimal, giving an extended life time due to a Ni content of 60 %.
  • the Hastelloy ® materials are considerably more costly than the Inconel ® alloy due to a high Mo content without giving an improved performance in HCl gas service.
  • HCl synthesis capacity 151.5 t/d (100 % HCl basis) giving a specific steam production of 0.65 t/t HCl produced, availabble at a condensation temperature of 170 °C.
  • Example 3 (according to the invention)
  • HCl synthesis reactor capacity 275 t/d (100 % HCl basis) giving a specific steam production of 1.0 t/t HCl produced, available at a condensation temperature of 235 °C.
  • HCl synthesis reactors accordingly to the present invention can be anticipated to have the same or better heat recovery performance for daily production rates of at least 500 tld of HCl (100 % basics)

Abstract

The invention concerns a method for the synthesis of HCl with energy recovery, where hydrogen and chlorine is supplied to a cooled synthesis furnace (2) with a burner section (1) and the produced HCl gas is absorbed in water. The cooling water for the synthesis furnace is used for production of steam. The energy is recovered as steam at a pressure above 2.8 MPa. It is preferred that the HCl gas is further cooled in a gas cooler (4) before the gas is absorbent in water. Preferably a gas cooler of the convective type is used where the HCl gas flows through the tube side of the gas cooler. It is also preferred that the cooling water for the gas cooler as well as the burner section is integrated in the steam generating system. A preferred construction material is an alloy with a Ni-content>30 %.

Description

Method and apparatus for synthesis of HCl The invention concerns a method and an apparatus for the synthesis of hydrogen chloride with increased and high value energy recovery.
For the synthesis of gaseous hydrogen chloride from the elements chlorine and hydrogen, the reaction mixture is combusted in a substantially hollow, cylindrical furnace, in the course of which considerable quantities of heat are produced . The hydrogen chloride gas produced is cooled and generally absorbed by water in an absorber that follows. The furnace used for performing the synthesis is usually made of graphite.
Several methods are known for recovering and utilising the heat liberated in the hydrogen chloride synthesis, for example the indirect cooling of the hydrogen chloride gas in heat exchange with a water circulation loop, as disclosed in German Patent No. DE-PS 857 343. The temperature increase limited to approximately 55 °C substantially restricts the utility of the heat.
In another method as described in German Patent No. DE-PS 33 13 761, it is known to cool hydrogen chloride gas in a first heat exchanger to approximately 200 °C with water carried in a circulation loop, to extract some of the absorption heat in a second heat exchange, and to effect flash evaporation of at least some of the heated water in heat exchange with the first. In this process, steam is produced at a temperature of approxi- mately 138° C and a vapour pressure of approximately 350 kPa which can be used industrially for instance as process steam.
German patent No. DE-PS 38 07 264 discloses a method and apparatus for generating saturated steam by the combustion of chlorine and hydrogen to produce hydrogen chloride gas. The apparatus includes an elongated synthesis furnace having an upper segment, a lower segment and a middle segment having a wall in the form of a heat exchanger. A heat transfer medium is circulated between the heat exchanger and a steam generator while heating the heat transfer medium to between 170° and 230 °C by heat exchange between the heat of the combustion and the heat transfer medium. Saturated steam is generated from water at a pressure of at least 700 kPa in the steam generator.
The object of the present invention is to increase the production capacity of HCl per unit. Another object is to recover produced energy efficiently at a higher temperature and pressure level than possible earlier. It is also an object of the invention to find more durable materials of construction which will result in less maintenance costs and longer life.
These and other objects of the invention are obtained with the method and apparatus as disclosed below, and the invention is further defined and characterised in the accompanying patent claims.
The invention thus concerns a method for the synthesis of HCl with energy recovery, where hydrogen and chlorine is supplied to a cooled synthesis furnace with a burner section and the produced HCl gas is absorbed in water. The cooling water for the synthesis furnace is used for production of steam. The energy is recovered as steam at a pressure above 2.8 MPa. It is preferred that the HCl gas is further cooled in a gas cooler before the gas is absorbed in water. Preferably a gas cooler of the convective type is used where the HCl gas flows through the tube side of the gas cooler. It is also preferred that the cooling water for the gas cooler as well as the burner section is integrated in the steam generating system.
The invention also includes an apparatus for the synthesis of HCl with energy recovery comprising a burner section, a combustion chamber, an absorber and a steam generator, wherein a gas cooler is arranged between the combustion chamber and the absorber. Preferably a gas cooler of the convective type is used where the HCl gas flows through the tube side of the gas cooler. The wall of the combustion chamber constitutes a heat exchanger made up of vertical tubes connected with bars preferably fixed off the centerline between the tubes. It is preferred to use construction materials of alloy with a high Ni content.
In existing technology the apparatus is essentially made of graphite or steel, and this leads to limitations concerning the quality of recovered energy, i.e. vapour temperature and pressure. Furthermore, the method of producing the graphite elements sets a limitation with regard to the maximum size of the separate units of the furnace that can be manufactured.
According to the present invention, it is possible to build essentially larger furnaces with a heat recovery at a much higher pressure level and with improved efficiency with regard to energy recovery. This is obtained by replacing graphite as a construction material with a metal alloy rich in nickel, and at the same time cooling the produced hydrogen chloride gas to a lower temperature than used in existing technology.
The invention will be further described with reference to the Figures 1-2, where
Figure 1 shows a HCl synthesis reactor with integrated heat recovery system.
Figure 2 A shows a wall of the combustion chamber with center welded bars.
Figure 2B shows a wall of the combustion chamber with off-center arrangement of flat bars.
As shown in figure 1, in the synthesis process hydrogen and chlorine are fed to a burner section 1, situated at the lower part of the furnace 2, from a controlled pressure source and at controlled rates. Above the burner the gases are ignited and burn to produce hydrogen chloride gas. The hydrogen chloride gas at a flame temperature of above 2000 °C flows through the combustion chamber 3 to a gas cooler 4 and into an absorber 5, where it is absorbed in water or dilute acid 6 to form hydrochloric acid at the required strength. By installing a gas cooler 4 after the furnace, the heat load for the following absorber is reduced and the size of this unit can be reduced accordingly. The product acid 7 flows into a tank at atmospheric pressure (not shown). The residual unabsorbed gas 8 is fed to a scrubber counter-current to the absorption water (not shown). The gas cooler 4 used is preferably of a convective type, and the hydrogen chloride gas should flow through the tube side of the cooler. The heat generated in the synthesis process is removed by circulating pressurized water and recovered as energy in steam at high temperature and pressure. Water is circulated between the heat exchanger forming the wall of the combustion chamber and a steam generator (steam drum) 9 where steam is produced. The cooling water for the gas cooler 4 is also integrated in the steam generating system, thereby giving increased energy recovery. In addition, heat is also recovered from the burner section 1 as an integrated part of the steam generation system.
The wall of the combustion chamber 3 forms a heat exchanger and is made up of vertical tubes 10, for circulation of water, that are interconnected by flat bar strips 11. A conventional arrangement is to have the flat bars center to center between the tubes. This is illustrated in Figure 2A. Due to varying stress in the bar and tube, there will be axial strain in the middle of the bar and the inner part of the tubes, and stress at the outer side of the tubes.
An alternative construction is shown in Figure 2 B where the bars are welded off the centerline between the pipes. The advantage of the latter arrangement is higher mechanical strength of the wall due to lower heat stress at a given heat load. Thereby the temperature differences in bars and pipes are reduced, and the heat recovered by the cooling medium will increase. In addition, the manufacture is less complicated, since the tube wall needs welding on only one side, in contrast to the center arrangement where welding on both sides is required.
At a given set of design parameters the combustion chamber can withstand a 25 kPa(g) inner reactor pressure when flat bars are welded centric to the tubes. With the flat bars welded off-centre, the construction can withstand 50 kPa(g) inner pressure due to less thermal stress on the flat bars. By putting buck stays at two meters distance around the reactor, the explosion pressure can be 2 barg in the reactor without serious damages to the construction.
The above conditions have been simulated by FVM (Finite Volume Method) calculations using the FLUENT software (available from Fluent Inc., Lebanon, NH03766-1442, USA), and further supported by mechanical stress calculations for the two wall configurations as shown in Figure 2A and 2B respectively. The construction material for the apparatus is important. In HCl gas (no condensation) it is possible to use carbon steel (boiler grade) up to a material temperature of about 150-160 °C with a life expectancy of the material of 2-3 years. For applications above 200 °C , specifically above 250 °C (which is required for production of >2.8MPa steam), materials with a high Ni content are required. Possible material can be Incoloy ® alloy 800/825, Inconel ® alloy 600 and various Hastelloy ® alloy qualities.
The Incoloy ® alloys may be borderline with respect to economic feasibility (cost of installation/ life expectancy) due to their relatively low Ni content of 30-40 %. The Inconel ® alloy is considered more optimal, giving an extended life time due to a Ni content of 60 %. The Hastelloy ® materials are considerably more costly than the Inconel ® alloy due to a high Mo content without giving an improved performance in HCl gas service.
In the Examples below typical steam production performance and corresponding HCl synthesis reactor capacity is given for existing technologies as well as the present invention.
Example 1 (not according to the invention)
Ref.: German patent No.: 3 313 761
Steam production: 1.8 t/hr at 350 kPa HCl synthesis reactor capacity: 41.2 t/d (100% HCl basis) giving a specific steam production of 1.05 t/t HCl produced, available at a condensation temperature of 138 °C.
Example 2 (not according to the invention)
Ref.: SGL Technik GmbH (Sigri)
Steam production: 4.1 t/hr at 800kPa
HCl synthesis capacity: 151.5 t/d (100 % HCl basis) giving a specific steam production of 0.65 t/t HCl produced, availabble at a condensation temperature of 170 °C. Example 3 (according to the invention)
Steam production: 11.4 t/hr at 3100 kPa
HCl synthesis reactor capacity: 275 t/d (100 % HCl basis) giving a specific steam production of 1.0 t/t HCl produced, available at a condensation temperature of 235 °C.
HCl synthesis reactors accordingly to the present invention can be anticipated to have the same or better heat recovery performance for daily production rates of at least 500 tld of HCl (100 % basics)

Claims

Patent claims
1. Method for the synthesis of HCl with energy recovery, where hydrogen and chlorine is supplied to a synthesis furnace (2) with a burner section (1) and the produced HCl gas is absorbed in water or dilute HCl, and where the cooling water for the synthesis furnace is used for production of steam, wherein the energy is recovered as steam at a pressure above 2.8 MPa.
2. Method according to claim 1 , wherein the HCl gas is further cooled in a gas cooler (4) before the gas is absorbed in water.
3. Method according to claim 2, wherein the gas cooler (4) used is of convective type and the HCl gas flows at the tube side of the gas cooler.
4. Method according to claim 2, wherein cooling water for the gas cooler is integrated in the steam generating system.
5. Method according to claim 1, wherein cooling water for the burner section is integrated in the steam generating system.
6. Apparatus for the synthesis of HCl with energy recovery, comprising a burner section (1), a combustion chamber (3), an absorber (5) and a steam generator (9), wherein a gas cooler (4) is arranged between the combustion chamber and the absorber.
7. Apparatus according to claim 6, wherein the wall of the combustion chamber (3) constitues a heat exchanger made up of vertical tubes (10) connected with bars (11) fixed off the centerline between the tubes.
8. Apparatus according to claim 6, wherein the gas cooler is of a convective type and the HCl gas will flow through the tube side of the gas cooler (4).
9. Apparatus according to claim 6, wherein the construction material is an alloy with a Ni-content > 30%.
PCT/NO2000/000313 1999-10-06 2000-09-22 METHOD AND APPARATUS FOR SYNTHESIS OF HCl WO2001025143A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU76928/00A AU7692800A (en) 1999-10-06 2000-09-22 Method and apparatus for synthesis of hcl

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NO19994856 1999-10-06
NO994856A NO994856L (en) 1999-10-06 1999-10-06 Method and apparatus for producing HC1

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EP1671926A1 (en) * 2004-12-15 2006-06-21 Sgl Carbon Ag Method for utilizing the cooling water of hydrogen chloride synthesis plants
WO2008111045A1 (en) * 2007-03-15 2008-09-18 Hcl Cleantech Ltd. A process for the recovery of hcl from a dilute solution thereof
CN101830437A (en) * 2009-05-25 2010-09-15 肖正群 Production method and device for synthesizing hydrogen chloride and concentrating alkali by using waste heat
CN102285670A (en) * 2011-06-16 2011-12-21 肖正群 Method and device for performing alkali concentration by utilizing synthesis waste heat of hydrogen chloride
WO2012131236A1 (en) * 2011-03-31 2012-10-04 Mersen France Py Sas Facility and reactor for directly synthesizing hydrochloric acid from hydrogen and chlorine with heat recovery
WO2012140472A1 (en) * 2011-04-12 2012-10-18 Cipolla Giuseppe Halogen-catalysed cold nuclear fusion
US8404355B2 (en) 2010-12-09 2013-03-26 Virdia Ltd Methods and systems for processing lignocellulosic materials and related compositions
US9115467B2 (en) 2010-08-01 2015-08-25 Virdia, Inc. Methods and systems for solvent purification
US9410216B2 (en) 2010-06-26 2016-08-09 Virdia, Inc. Sugar mixtures and methods for production and use thereof
US9476106B2 (en) 2010-06-28 2016-10-25 Virdia, Inc. Methods and systems for processing a sucrose crop and sugar mixtures
US9512495B2 (en) 2011-04-07 2016-12-06 Virdia, Inc. Lignocellulose conversion processes and products
US9617608B2 (en) 2011-10-10 2017-04-11 Virdia, Inc. Sugar compositions
US9663836B2 (en) 2010-09-02 2017-05-30 Virdia, Inc. Methods and systems for processing sugar mixtures and resultant compositions
CN111498807A (en) * 2020-04-14 2020-08-07 四川建筑职业技术学院 HCl synthesis furnace for producing steam, production system and production method
CN112661113A (en) * 2021-01-21 2021-04-16 新疆圣雄氯碱有限公司 Control method of hydrogen chloride synthesis furnace
CN112742182A (en) * 2020-12-22 2021-05-04 南通润中石墨设备有限公司 Gas-liquid separation system of HCL falling film absorber
US11078548B2 (en) 2015-01-07 2021-08-03 Virdia, Llc Method for producing xylitol by fermentation
CN114436215A (en) * 2021-12-29 2022-05-06 安徽华塑股份有限公司 Dehydrogenation process of hydrogen chloride synthesis gas
CN114673980A (en) * 2022-05-24 2022-06-28 东营市赫邦化工有限公司 Hydrogen chloride synthetic furnace byproduct steam device
US11376546B2 (en) * 2018-09-24 2022-07-05 Valmet Technologies Oy Method and a system for producing hydrochloric acid from flue gases

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JPH046247A (en) * 1990-04-23 1992-01-10 Nippon Steel Corp Steel for waste incineration furnace boiler
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Cited By (38)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1671926A1 (en) * 2004-12-15 2006-06-21 Sgl Carbon Ag Method for utilizing the cooling water of hydrogen chloride synthesis plants
WO2008111045A1 (en) * 2007-03-15 2008-09-18 Hcl Cleantech Ltd. A process for the recovery of hcl from a dilute solution thereof
AU2008224486B2 (en) * 2007-03-15 2011-10-20 Hcl Cleantech Ltd. A process for the recovery of HCl from a dilute solution thereof
CN101830437A (en) * 2009-05-25 2010-09-15 肖正群 Production method and device for synthesizing hydrogen chloride and concentrating alkali by using waste heat
US9410216B2 (en) 2010-06-26 2016-08-09 Virdia, Inc. Sugar mixtures and methods for production and use thereof
US9963673B2 (en) 2010-06-26 2018-05-08 Virdia, Inc. Sugar mixtures and methods for production and use thereof
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